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Figure 2-38. Typical nozzle connections. Figure 2-39. Typical self-reinforced nozzles. 88 Pressure Vessel Design Manual

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Page 1: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-38 Typical nozzle connectionsFigure 2-39 Typical self-reinforced nozzles

88 Pressure Vessel Design Manual

NOZZLE POSITION

NOZZLE IN HEAD ndash NORMAL TO WALL NOZZLE IN CONE ndash NORMAL TO WALL

NOZZLE IN CONE ndash INCLINED TO LONG AXIS

NOZZLE IN CONE ndash NORMAL TOCENTERLINE

NOZZLE IN FLAT HEAD ndash NORMAL TO HEAD

NOZZLE IN FLAT HEAD ndash ANGLEDNOZZLE IN SHELL ndash ANGLED

NOZZLE IN SHELL ndash ANGULAR OFFSET

NOZZLE IN SHELL ndash OFFSET AND NORMALTO CENTERLINE

NOZZLE IN SHELL ndash NORMAL TO WALL

NOZZLE IN HEAD ndash NORMAL OR PARALLEL TO VESSEL CENTERLINE

90deg

90deg

ANG

ANG

ANGANG

ANG

General Design 89

Procedure 2-13 Find or Revise the Center of Gravity of a Vessel

Notation

C frac14 distance to center of gravity ft or in

D0 frac14 revised distance to CG ft or indn frac14 distance from original CG to weights to add or

remove (thorn) or () as shown ft or inLn frac14 distance from REF line to CG of a component

weight ft or inWn frac14 weight of vessel component contents or attach-

ments lbW0 frac14 new overall weight lb W thorn or ndash

PWn

W frac14 overall weight lbP

Wn

un frac14 revised unit weights lb (thorn) to add weight(ndash) to remove weight

To find the CG

C frac14P

LnWn

W

To revise CG

D0 frac14 CP

dnun

W0

Procedure 2-14 Minimum Design Metal Temperature (MDMT)

Notation

R frac14 use the lesser of R1 or R2R1 frac14 ratio of thickness required at MDMT to the

corroded thicknessR2 frac14 ratio of the actual stress to the allowable

stresstMT frac14 thickness required of the part at MDMT intDT frac14 thickness required of the part at design temper-

ature intn frac14 thickness of the part new in (exclusive of

thinning allowance for heads and undertolerancefor pipe)

tc frac14 thickness of the part corroded inCa frac14 corrosion allowance inE frac14 joint efficiency

SMT frac14 allowable stress at MDMT psiSDT frac14 allowable stress at design temperature psiSa frac14 actual tension stress in part due to pressure and

all loadings psi

T1 frac14 lowest allowable temperature for a given partbased on the appropriate material curve ofFigure 2-43 degrees F

T2 frac14 reduction in MDMT without impact testing perFigure 2-42 degrees F

This MDMT procedure is used to determine the lowestpermissible temperature for which charpy impact testing isor is not required The ASME Code requires this be deter-mined for every pressure vessel and theMDMT be stampedon the nameplate While every pressure vessel has its ownunique MDMT this may or may not be the MDMT that isstamped on the nameplate Not only does every pressurevessel have its own uniqueMDMT but every component ofthat pressure vessel has an MDMT The vessel MDMT isthe highest temperature of all the component MDMTrsquos Onoccasion the MDMT is specified by the end user as anarbitrary value The vessel fabricator is then responsible toverify that the actual MDMT of every component used inthat pressure vessel is lower than the arbitrary value

Figure 2-40 Load diagram for a typical vertical vessel

90 Pressure Vessel Design Manual

requested for the nameplate stamping Considering thisthere are various definitions for MDMT depending on howit is used The definitions follow

1 Arbitrary MDMT A discretionary arbitrarytemperature specified by a user or client or deter-mined in accordance with the provisions of UG-20Some users have a standard value that has beenchosen as the lowest mean temperature of the siteconditions such as 15F

2 Exemption MDMT The lowest temperature atwhich the pressure vessel may be operated at fulldesign pressure without impact testing of thecomponent parts

3 Test MDMT The temperature at which the vessel ischarpy impact tested

The ASME Code rules for MDMT are built arounda set of material exemption curves as shown inFigure 2-43 These curves account for the differenttoughness characteristics of carbon and low alloy steel anddetermine at what temperature and corresponding thick-ness impact testing will become mandatory

There is an additional exemption curve (see Figure 2-42)which allows a decrease in theMDMTof every componentand thus the vessel depending on one of several ratiosspecified This curve would permit carbon steel withoutimpact testing to be used at a temperature of ()150F

provided the combined stresses are less than 40 of theallowable stress for that material Granted the vessel wouldbemore than twice as thick as it needed to be for the pressurecondition alone but if the goal was to exempt the vesselfrom impact testing it could be accomplished

Since impact testing is a major expense to the manu-facturer of a pressure vessel the designer should doeverything to avoid it Impact testing can always be avoidedbut may not be the most economical alternative Followingthese steps will help eliminate the need for impact testingand at the same time will provide the lowest MDMT

1 Upgrade the material to a higher group2 Increase the thickness of the component to reduce

the stress in the part3 Decrease the pressure at MDMT This is a process

change and may or may not be possible Sometimesa vessel does not operate at full design pressure atthe low temperature condition but has alternateconditions such as shutdown or depressurizationThese alternate low temperature conditions can alsobe stamped on the nameplate

Formulas

R1 frac14 trEtc

Table 2-7Determination of MDMT (Example)

Part Material

Material

Group

SMT

ksi

SDT

ksi tn

tDT(3)

tMT

(3) tc

Sa

ksi R1 R2 T1 T2

MDMTF

Shell SA-516-70 B 175 166 100 0869 0823 0875 1397 0799 0798 31 201 thorn11

Head(1) SA-516-70 B 175 166 0857 0653 0620 0732 1489 0847 0851 218 15 thorn7

1000 Noz(2) SA-53-B B 128 122 0519 0174 0166 0394 526 0421 0410 e518 59

1000 300 Flg (4) SA-105 B 175 166 0519 0128 0121 0394 526 0307 0300 e518 70

3000 Blind (5) SA-266-2 B 175 166 606 d 148 594 d d d 51 105 e54

3000 Body Flg SA-266-2 B 175 166 Same as Shell thorn11

Wear PL SA-516-70 B 175 166 100 d d 100 d d d d d thorn11(6)

Bolting SA-193-B7 d d d d d d d d d d d d e40

Notes

1 The governing thickness for heads is based on that portion of the head which is in tension For a 21 SE head this is the crown position where R frac14 090

2 Includes pipe 12frac12 under tolerance

3 Thickness exclusive of Ca

4 Thickness at the hub (weld attachment) governs

5 The governing thickness of flat heads and blind flanges is 14 of actual thickness

6 Since the tension stress in the wear plate is less than the tension stress in the shell the MDMT for the shell will govern

General Design 91

R2 frac14 SaSMT

tc frac14 tn Ca

T2 frac14 eth1 RTHORN100MDMT frac14 T1 T2

Procedure

Step 1 Determine the lowest anticipated temperature towhich the vessel will be subjected

Step 2 Compare the lowest combined pressure-temperaturecase with the MDMT for each component

Step 3 Determine if any components must be impacttested in their proposed material grade and thicknessThis would establish the MDMT

Step 4 Establish the overall MDMT as the highest value ofMDMT for each of the component parts

Notes

1 For flat heads tubesheets and blind flanges thethickness used for each of the respective thicknessrsquois that thickness divided by 4

2 For corner fillet or lap-welded joints the thicknessused shall be the thinner of the two parts being joined

3 For butt joints the thickness used shall be thethickest joint

4 For any Code construction if the vessel isstress relieved and that stress relieving was nota Code requirement the MDMT for that vessel maybe reduced by 30 without impact testing

Design Conditions (for example)DT frac14 700FP frac14 400 PSIGCa frac14 0125Ri frac14 30 inE (Shell) frac14 085E (Head) frac14 100MDMT for vessel frac14 thorn 11F

General Notes on Assignment of Materials to Curves(Reprinted with permission from ASME Code SectionVIII Div 1)

a Curve Adall carbon and all low alloy steel platesstructural shapes and bars not listed in Curves B Cand D below

b Curve B

1 SA-285 Grades A and BSA-414 Grade ASA-515 Grade 60SA-516 Grades 65 and 70 if not normalizedSA-612 if not normalizedSA-662 Grade B if not normalized

2 all materials of Curve A if produced to fine grainpractice and normalized which are not listed forCurves C and D below

3 except for bolting (see (e) below) platesstructural shapes and bars all other productforms (such as pipe fittings forgings castingsand tubing) not listed for Curves C and Dbelow

4 parts permitted under UG-11 shall be includedin Curve B even when fabricated from plate thatotherwise would be assigned to a differentcurve

c Curve C1 SA-182 Grades F21 and F22 if normalized and

temperedSA-302 Grades C and DSA-336 Grades F21 and F22 if normalized andtemperedSA-387 Grades 21 and 22 if normalized andtemperedSA-516 Grades 55 and 60 if not normalizedSA-533 Grades B and CSA-662 Grade A

2 all materials of Curve B if produced to fine grainpractice and normalized and not listed for CurveD below

Figure 2-41 Dimensions of vessel used for MDMTexample

92 Pressure Vessel Design Manual

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 2: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

NOZZLE POSITION

NOZZLE IN HEAD ndash NORMAL TO WALL NOZZLE IN CONE ndash NORMAL TO WALL

NOZZLE IN CONE ndash INCLINED TO LONG AXIS

NOZZLE IN CONE ndash NORMAL TOCENTERLINE

NOZZLE IN FLAT HEAD ndash NORMAL TO HEAD

NOZZLE IN FLAT HEAD ndash ANGLEDNOZZLE IN SHELL ndash ANGLED

NOZZLE IN SHELL ndash ANGULAR OFFSET

NOZZLE IN SHELL ndash OFFSET AND NORMALTO CENTERLINE

NOZZLE IN SHELL ndash NORMAL TO WALL

NOZZLE IN HEAD ndash NORMAL OR PARALLEL TO VESSEL CENTERLINE

90deg

90deg

ANG

ANG

ANGANG

ANG

General Design 89

Procedure 2-13 Find or Revise the Center of Gravity of a Vessel

Notation

C frac14 distance to center of gravity ft or in

D0 frac14 revised distance to CG ft or indn frac14 distance from original CG to weights to add or

remove (thorn) or () as shown ft or inLn frac14 distance from REF line to CG of a component

weight ft or inWn frac14 weight of vessel component contents or attach-

ments lbW0 frac14 new overall weight lb W thorn or ndash

PWn

W frac14 overall weight lbP

Wn

un frac14 revised unit weights lb (thorn) to add weight(ndash) to remove weight

To find the CG

C frac14P

LnWn

W

To revise CG

D0 frac14 CP

dnun

W0

Procedure 2-14 Minimum Design Metal Temperature (MDMT)

Notation

R frac14 use the lesser of R1 or R2R1 frac14 ratio of thickness required at MDMT to the

corroded thicknessR2 frac14 ratio of the actual stress to the allowable

stresstMT frac14 thickness required of the part at MDMT intDT frac14 thickness required of the part at design temper-

ature intn frac14 thickness of the part new in (exclusive of

thinning allowance for heads and undertolerancefor pipe)

tc frac14 thickness of the part corroded inCa frac14 corrosion allowance inE frac14 joint efficiency

SMT frac14 allowable stress at MDMT psiSDT frac14 allowable stress at design temperature psiSa frac14 actual tension stress in part due to pressure and

all loadings psi

T1 frac14 lowest allowable temperature for a given partbased on the appropriate material curve ofFigure 2-43 degrees F

T2 frac14 reduction in MDMT without impact testing perFigure 2-42 degrees F

This MDMT procedure is used to determine the lowestpermissible temperature for which charpy impact testing isor is not required The ASME Code requires this be deter-mined for every pressure vessel and theMDMT be stampedon the nameplate While every pressure vessel has its ownunique MDMT this may or may not be the MDMT that isstamped on the nameplate Not only does every pressurevessel have its own uniqueMDMT but every component ofthat pressure vessel has an MDMT The vessel MDMT isthe highest temperature of all the component MDMTrsquos Onoccasion the MDMT is specified by the end user as anarbitrary value The vessel fabricator is then responsible toverify that the actual MDMT of every component used inthat pressure vessel is lower than the arbitrary value

Figure 2-40 Load diagram for a typical vertical vessel

90 Pressure Vessel Design Manual

requested for the nameplate stamping Considering thisthere are various definitions for MDMT depending on howit is used The definitions follow

1 Arbitrary MDMT A discretionary arbitrarytemperature specified by a user or client or deter-mined in accordance with the provisions of UG-20Some users have a standard value that has beenchosen as the lowest mean temperature of the siteconditions such as 15F

2 Exemption MDMT The lowest temperature atwhich the pressure vessel may be operated at fulldesign pressure without impact testing of thecomponent parts

3 Test MDMT The temperature at which the vessel ischarpy impact tested

The ASME Code rules for MDMT are built arounda set of material exemption curves as shown inFigure 2-43 These curves account for the differenttoughness characteristics of carbon and low alloy steel anddetermine at what temperature and corresponding thick-ness impact testing will become mandatory

There is an additional exemption curve (see Figure 2-42)which allows a decrease in theMDMTof every componentand thus the vessel depending on one of several ratiosspecified This curve would permit carbon steel withoutimpact testing to be used at a temperature of ()150F

provided the combined stresses are less than 40 of theallowable stress for that material Granted the vessel wouldbemore than twice as thick as it needed to be for the pressurecondition alone but if the goal was to exempt the vesselfrom impact testing it could be accomplished

Since impact testing is a major expense to the manu-facturer of a pressure vessel the designer should doeverything to avoid it Impact testing can always be avoidedbut may not be the most economical alternative Followingthese steps will help eliminate the need for impact testingand at the same time will provide the lowest MDMT

1 Upgrade the material to a higher group2 Increase the thickness of the component to reduce

the stress in the part3 Decrease the pressure at MDMT This is a process

change and may or may not be possible Sometimesa vessel does not operate at full design pressure atthe low temperature condition but has alternateconditions such as shutdown or depressurizationThese alternate low temperature conditions can alsobe stamped on the nameplate

Formulas

R1 frac14 trEtc

Table 2-7Determination of MDMT (Example)

Part Material

Material

Group

SMT

ksi

SDT

ksi tn

tDT(3)

tMT

(3) tc

Sa

ksi R1 R2 T1 T2

MDMTF

Shell SA-516-70 B 175 166 100 0869 0823 0875 1397 0799 0798 31 201 thorn11

Head(1) SA-516-70 B 175 166 0857 0653 0620 0732 1489 0847 0851 218 15 thorn7

1000 Noz(2) SA-53-B B 128 122 0519 0174 0166 0394 526 0421 0410 e518 59

1000 300 Flg (4) SA-105 B 175 166 0519 0128 0121 0394 526 0307 0300 e518 70

3000 Blind (5) SA-266-2 B 175 166 606 d 148 594 d d d 51 105 e54

3000 Body Flg SA-266-2 B 175 166 Same as Shell thorn11

Wear PL SA-516-70 B 175 166 100 d d 100 d d d d d thorn11(6)

Bolting SA-193-B7 d d d d d d d d d d d d e40

Notes

1 The governing thickness for heads is based on that portion of the head which is in tension For a 21 SE head this is the crown position where R frac14 090

2 Includes pipe 12frac12 under tolerance

3 Thickness exclusive of Ca

4 Thickness at the hub (weld attachment) governs

5 The governing thickness of flat heads and blind flanges is 14 of actual thickness

6 Since the tension stress in the wear plate is less than the tension stress in the shell the MDMT for the shell will govern

General Design 91

R2 frac14 SaSMT

tc frac14 tn Ca

T2 frac14 eth1 RTHORN100MDMT frac14 T1 T2

Procedure

Step 1 Determine the lowest anticipated temperature towhich the vessel will be subjected

Step 2 Compare the lowest combined pressure-temperaturecase with the MDMT for each component

Step 3 Determine if any components must be impacttested in their proposed material grade and thicknessThis would establish the MDMT

Step 4 Establish the overall MDMT as the highest value ofMDMT for each of the component parts

Notes

1 For flat heads tubesheets and blind flanges thethickness used for each of the respective thicknessrsquois that thickness divided by 4

2 For corner fillet or lap-welded joints the thicknessused shall be the thinner of the two parts being joined

3 For butt joints the thickness used shall be thethickest joint

4 For any Code construction if the vessel isstress relieved and that stress relieving was nota Code requirement the MDMT for that vessel maybe reduced by 30 without impact testing

Design Conditions (for example)DT frac14 700FP frac14 400 PSIGCa frac14 0125Ri frac14 30 inE (Shell) frac14 085E (Head) frac14 100MDMT for vessel frac14 thorn 11F

General Notes on Assignment of Materials to Curves(Reprinted with permission from ASME Code SectionVIII Div 1)

a Curve Adall carbon and all low alloy steel platesstructural shapes and bars not listed in Curves B Cand D below

b Curve B

1 SA-285 Grades A and BSA-414 Grade ASA-515 Grade 60SA-516 Grades 65 and 70 if not normalizedSA-612 if not normalizedSA-662 Grade B if not normalized

2 all materials of Curve A if produced to fine grainpractice and normalized which are not listed forCurves C and D below

3 except for bolting (see (e) below) platesstructural shapes and bars all other productforms (such as pipe fittings forgings castingsand tubing) not listed for Curves C and Dbelow

4 parts permitted under UG-11 shall be includedin Curve B even when fabricated from plate thatotherwise would be assigned to a differentcurve

c Curve C1 SA-182 Grades F21 and F22 if normalized and

temperedSA-302 Grades C and DSA-336 Grades F21 and F22 if normalized andtemperedSA-387 Grades 21 and 22 if normalized andtemperedSA-516 Grades 55 and 60 if not normalizedSA-533 Grades B and CSA-662 Grade A

2 all materials of Curve B if produced to fine grainpractice and normalized and not listed for CurveD below

Figure 2-41 Dimensions of vessel used for MDMTexample

92 Pressure Vessel Design Manual

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 3: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Procedure 2-13 Find or Revise the Center of Gravity of a Vessel

Notation

C frac14 distance to center of gravity ft or in

D0 frac14 revised distance to CG ft or indn frac14 distance from original CG to weights to add or

remove (thorn) or () as shown ft or inLn frac14 distance from REF line to CG of a component

weight ft or inWn frac14 weight of vessel component contents or attach-

ments lbW0 frac14 new overall weight lb W thorn or ndash

PWn

W frac14 overall weight lbP

Wn

un frac14 revised unit weights lb (thorn) to add weight(ndash) to remove weight

To find the CG

C frac14P

LnWn

W

To revise CG

D0 frac14 CP

dnun

W0

Procedure 2-14 Minimum Design Metal Temperature (MDMT)

Notation

R frac14 use the lesser of R1 or R2R1 frac14 ratio of thickness required at MDMT to the

corroded thicknessR2 frac14 ratio of the actual stress to the allowable

stresstMT frac14 thickness required of the part at MDMT intDT frac14 thickness required of the part at design temper-

ature intn frac14 thickness of the part new in (exclusive of

thinning allowance for heads and undertolerancefor pipe)

tc frac14 thickness of the part corroded inCa frac14 corrosion allowance inE frac14 joint efficiency

SMT frac14 allowable stress at MDMT psiSDT frac14 allowable stress at design temperature psiSa frac14 actual tension stress in part due to pressure and

all loadings psi

T1 frac14 lowest allowable temperature for a given partbased on the appropriate material curve ofFigure 2-43 degrees F

T2 frac14 reduction in MDMT without impact testing perFigure 2-42 degrees F

This MDMT procedure is used to determine the lowestpermissible temperature for which charpy impact testing isor is not required The ASME Code requires this be deter-mined for every pressure vessel and theMDMT be stampedon the nameplate While every pressure vessel has its ownunique MDMT this may or may not be the MDMT that isstamped on the nameplate Not only does every pressurevessel have its own uniqueMDMT but every component ofthat pressure vessel has an MDMT The vessel MDMT isthe highest temperature of all the component MDMTrsquos Onoccasion the MDMT is specified by the end user as anarbitrary value The vessel fabricator is then responsible toverify that the actual MDMT of every component used inthat pressure vessel is lower than the arbitrary value

Figure 2-40 Load diagram for a typical vertical vessel

90 Pressure Vessel Design Manual

requested for the nameplate stamping Considering thisthere are various definitions for MDMT depending on howit is used The definitions follow

1 Arbitrary MDMT A discretionary arbitrarytemperature specified by a user or client or deter-mined in accordance with the provisions of UG-20Some users have a standard value that has beenchosen as the lowest mean temperature of the siteconditions such as 15F

2 Exemption MDMT The lowest temperature atwhich the pressure vessel may be operated at fulldesign pressure without impact testing of thecomponent parts

3 Test MDMT The temperature at which the vessel ischarpy impact tested

The ASME Code rules for MDMT are built arounda set of material exemption curves as shown inFigure 2-43 These curves account for the differenttoughness characteristics of carbon and low alloy steel anddetermine at what temperature and corresponding thick-ness impact testing will become mandatory

There is an additional exemption curve (see Figure 2-42)which allows a decrease in theMDMTof every componentand thus the vessel depending on one of several ratiosspecified This curve would permit carbon steel withoutimpact testing to be used at a temperature of ()150F

provided the combined stresses are less than 40 of theallowable stress for that material Granted the vessel wouldbemore than twice as thick as it needed to be for the pressurecondition alone but if the goal was to exempt the vesselfrom impact testing it could be accomplished

Since impact testing is a major expense to the manu-facturer of a pressure vessel the designer should doeverything to avoid it Impact testing can always be avoidedbut may not be the most economical alternative Followingthese steps will help eliminate the need for impact testingand at the same time will provide the lowest MDMT

1 Upgrade the material to a higher group2 Increase the thickness of the component to reduce

the stress in the part3 Decrease the pressure at MDMT This is a process

change and may or may not be possible Sometimesa vessel does not operate at full design pressure atthe low temperature condition but has alternateconditions such as shutdown or depressurizationThese alternate low temperature conditions can alsobe stamped on the nameplate

Formulas

R1 frac14 trEtc

Table 2-7Determination of MDMT (Example)

Part Material

Material

Group

SMT

ksi

SDT

ksi tn

tDT(3)

tMT

(3) tc

Sa

ksi R1 R2 T1 T2

MDMTF

Shell SA-516-70 B 175 166 100 0869 0823 0875 1397 0799 0798 31 201 thorn11

Head(1) SA-516-70 B 175 166 0857 0653 0620 0732 1489 0847 0851 218 15 thorn7

1000 Noz(2) SA-53-B B 128 122 0519 0174 0166 0394 526 0421 0410 e518 59

1000 300 Flg (4) SA-105 B 175 166 0519 0128 0121 0394 526 0307 0300 e518 70

3000 Blind (5) SA-266-2 B 175 166 606 d 148 594 d d d 51 105 e54

3000 Body Flg SA-266-2 B 175 166 Same as Shell thorn11

Wear PL SA-516-70 B 175 166 100 d d 100 d d d d d thorn11(6)

Bolting SA-193-B7 d d d d d d d d d d d d e40

Notes

1 The governing thickness for heads is based on that portion of the head which is in tension For a 21 SE head this is the crown position where R frac14 090

2 Includes pipe 12frac12 under tolerance

3 Thickness exclusive of Ca

4 Thickness at the hub (weld attachment) governs

5 The governing thickness of flat heads and blind flanges is 14 of actual thickness

6 Since the tension stress in the wear plate is less than the tension stress in the shell the MDMT for the shell will govern

General Design 91

R2 frac14 SaSMT

tc frac14 tn Ca

T2 frac14 eth1 RTHORN100MDMT frac14 T1 T2

Procedure

Step 1 Determine the lowest anticipated temperature towhich the vessel will be subjected

Step 2 Compare the lowest combined pressure-temperaturecase with the MDMT for each component

Step 3 Determine if any components must be impacttested in their proposed material grade and thicknessThis would establish the MDMT

Step 4 Establish the overall MDMT as the highest value ofMDMT for each of the component parts

Notes

1 For flat heads tubesheets and blind flanges thethickness used for each of the respective thicknessrsquois that thickness divided by 4

2 For corner fillet or lap-welded joints the thicknessused shall be the thinner of the two parts being joined

3 For butt joints the thickness used shall be thethickest joint

4 For any Code construction if the vessel isstress relieved and that stress relieving was nota Code requirement the MDMT for that vessel maybe reduced by 30 without impact testing

Design Conditions (for example)DT frac14 700FP frac14 400 PSIGCa frac14 0125Ri frac14 30 inE (Shell) frac14 085E (Head) frac14 100MDMT for vessel frac14 thorn 11F

General Notes on Assignment of Materials to Curves(Reprinted with permission from ASME Code SectionVIII Div 1)

a Curve Adall carbon and all low alloy steel platesstructural shapes and bars not listed in Curves B Cand D below

b Curve B

1 SA-285 Grades A and BSA-414 Grade ASA-515 Grade 60SA-516 Grades 65 and 70 if not normalizedSA-612 if not normalizedSA-662 Grade B if not normalized

2 all materials of Curve A if produced to fine grainpractice and normalized which are not listed forCurves C and D below

3 except for bolting (see (e) below) platesstructural shapes and bars all other productforms (such as pipe fittings forgings castingsand tubing) not listed for Curves C and Dbelow

4 parts permitted under UG-11 shall be includedin Curve B even when fabricated from plate thatotherwise would be assigned to a differentcurve

c Curve C1 SA-182 Grades F21 and F22 if normalized and

temperedSA-302 Grades C and DSA-336 Grades F21 and F22 if normalized andtemperedSA-387 Grades 21 and 22 if normalized andtemperedSA-516 Grades 55 and 60 if not normalizedSA-533 Grades B and CSA-662 Grade A

2 all materials of Curve B if produced to fine grainpractice and normalized and not listed for CurveD below

Figure 2-41 Dimensions of vessel used for MDMTexample

92 Pressure Vessel Design Manual

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 4: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

requested for the nameplate stamping Considering thisthere are various definitions for MDMT depending on howit is used The definitions follow

1 Arbitrary MDMT A discretionary arbitrarytemperature specified by a user or client or deter-mined in accordance with the provisions of UG-20Some users have a standard value that has beenchosen as the lowest mean temperature of the siteconditions such as 15F

2 Exemption MDMT The lowest temperature atwhich the pressure vessel may be operated at fulldesign pressure without impact testing of thecomponent parts

3 Test MDMT The temperature at which the vessel ischarpy impact tested

The ASME Code rules for MDMT are built arounda set of material exemption curves as shown inFigure 2-43 These curves account for the differenttoughness characteristics of carbon and low alloy steel anddetermine at what temperature and corresponding thick-ness impact testing will become mandatory

There is an additional exemption curve (see Figure 2-42)which allows a decrease in theMDMTof every componentand thus the vessel depending on one of several ratiosspecified This curve would permit carbon steel withoutimpact testing to be used at a temperature of ()150F

provided the combined stresses are less than 40 of theallowable stress for that material Granted the vessel wouldbemore than twice as thick as it needed to be for the pressurecondition alone but if the goal was to exempt the vesselfrom impact testing it could be accomplished

Since impact testing is a major expense to the manu-facturer of a pressure vessel the designer should doeverything to avoid it Impact testing can always be avoidedbut may not be the most economical alternative Followingthese steps will help eliminate the need for impact testingand at the same time will provide the lowest MDMT

1 Upgrade the material to a higher group2 Increase the thickness of the component to reduce

the stress in the part3 Decrease the pressure at MDMT This is a process

change and may or may not be possible Sometimesa vessel does not operate at full design pressure atthe low temperature condition but has alternateconditions such as shutdown or depressurizationThese alternate low temperature conditions can alsobe stamped on the nameplate

Formulas

R1 frac14 trEtc

Table 2-7Determination of MDMT (Example)

Part Material

Material

Group

SMT

ksi

SDT

ksi tn

tDT(3)

tMT

(3) tc

Sa

ksi R1 R2 T1 T2

MDMTF

Shell SA-516-70 B 175 166 100 0869 0823 0875 1397 0799 0798 31 201 thorn11

Head(1) SA-516-70 B 175 166 0857 0653 0620 0732 1489 0847 0851 218 15 thorn7

1000 Noz(2) SA-53-B B 128 122 0519 0174 0166 0394 526 0421 0410 e518 59

1000 300 Flg (4) SA-105 B 175 166 0519 0128 0121 0394 526 0307 0300 e518 70

3000 Blind (5) SA-266-2 B 175 166 606 d 148 594 d d d 51 105 e54

3000 Body Flg SA-266-2 B 175 166 Same as Shell thorn11

Wear PL SA-516-70 B 175 166 100 d d 100 d d d d d thorn11(6)

Bolting SA-193-B7 d d d d d d d d d d d d e40

Notes

1 The governing thickness for heads is based on that portion of the head which is in tension For a 21 SE head this is the crown position where R frac14 090

2 Includes pipe 12frac12 under tolerance

3 Thickness exclusive of Ca

4 Thickness at the hub (weld attachment) governs

5 The governing thickness of flat heads and blind flanges is 14 of actual thickness

6 Since the tension stress in the wear plate is less than the tension stress in the shell the MDMT for the shell will govern

General Design 91

R2 frac14 SaSMT

tc frac14 tn Ca

T2 frac14 eth1 RTHORN100MDMT frac14 T1 T2

Procedure

Step 1 Determine the lowest anticipated temperature towhich the vessel will be subjected

Step 2 Compare the lowest combined pressure-temperaturecase with the MDMT for each component

Step 3 Determine if any components must be impacttested in their proposed material grade and thicknessThis would establish the MDMT

Step 4 Establish the overall MDMT as the highest value ofMDMT for each of the component parts

Notes

1 For flat heads tubesheets and blind flanges thethickness used for each of the respective thicknessrsquois that thickness divided by 4

2 For corner fillet or lap-welded joints the thicknessused shall be the thinner of the two parts being joined

3 For butt joints the thickness used shall be thethickest joint

4 For any Code construction if the vessel isstress relieved and that stress relieving was nota Code requirement the MDMT for that vessel maybe reduced by 30 without impact testing

Design Conditions (for example)DT frac14 700FP frac14 400 PSIGCa frac14 0125Ri frac14 30 inE (Shell) frac14 085E (Head) frac14 100MDMT for vessel frac14 thorn 11F

General Notes on Assignment of Materials to Curves(Reprinted with permission from ASME Code SectionVIII Div 1)

a Curve Adall carbon and all low alloy steel platesstructural shapes and bars not listed in Curves B Cand D below

b Curve B

1 SA-285 Grades A and BSA-414 Grade ASA-515 Grade 60SA-516 Grades 65 and 70 if not normalizedSA-612 if not normalizedSA-662 Grade B if not normalized

2 all materials of Curve A if produced to fine grainpractice and normalized which are not listed forCurves C and D below

3 except for bolting (see (e) below) platesstructural shapes and bars all other productforms (such as pipe fittings forgings castingsand tubing) not listed for Curves C and Dbelow

4 parts permitted under UG-11 shall be includedin Curve B even when fabricated from plate thatotherwise would be assigned to a differentcurve

c Curve C1 SA-182 Grades F21 and F22 if normalized and

temperedSA-302 Grades C and DSA-336 Grades F21 and F22 if normalized andtemperedSA-387 Grades 21 and 22 if normalized andtemperedSA-516 Grades 55 and 60 if not normalizedSA-533 Grades B and CSA-662 Grade A

2 all materials of Curve B if produced to fine grainpractice and normalized and not listed for CurveD below

Figure 2-41 Dimensions of vessel used for MDMTexample

92 Pressure Vessel Design Manual

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 5: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

R2 frac14 SaSMT

tc frac14 tn Ca

T2 frac14 eth1 RTHORN100MDMT frac14 T1 T2

Procedure

Step 1 Determine the lowest anticipated temperature towhich the vessel will be subjected

Step 2 Compare the lowest combined pressure-temperaturecase with the MDMT for each component

Step 3 Determine if any components must be impacttested in their proposed material grade and thicknessThis would establish the MDMT

Step 4 Establish the overall MDMT as the highest value ofMDMT for each of the component parts

Notes

1 For flat heads tubesheets and blind flanges thethickness used for each of the respective thicknessrsquois that thickness divided by 4

2 For corner fillet or lap-welded joints the thicknessused shall be the thinner of the two parts being joined

3 For butt joints the thickness used shall be thethickest joint

4 For any Code construction if the vessel isstress relieved and that stress relieving was nota Code requirement the MDMT for that vessel maybe reduced by 30 without impact testing

Design Conditions (for example)DT frac14 700FP frac14 400 PSIGCa frac14 0125Ri frac14 30 inE (Shell) frac14 085E (Head) frac14 100MDMT for vessel frac14 thorn 11F

General Notes on Assignment of Materials to Curves(Reprinted with permission from ASME Code SectionVIII Div 1)

a Curve Adall carbon and all low alloy steel platesstructural shapes and bars not listed in Curves B Cand D below

b Curve B

1 SA-285 Grades A and BSA-414 Grade ASA-515 Grade 60SA-516 Grades 65 and 70 if not normalizedSA-612 if not normalizedSA-662 Grade B if not normalized

2 all materials of Curve A if produced to fine grainpractice and normalized which are not listed forCurves C and D below

3 except for bolting (see (e) below) platesstructural shapes and bars all other productforms (such as pipe fittings forgings castingsand tubing) not listed for Curves C and Dbelow

4 parts permitted under UG-11 shall be includedin Curve B even when fabricated from plate thatotherwise would be assigned to a differentcurve

c Curve C1 SA-182 Grades F21 and F22 if normalized and

temperedSA-302 Grades C and DSA-336 Grades F21 and F22 if normalized andtemperedSA-387 Grades 21 and 22 if normalized andtemperedSA-516 Grades 55 and 60 if not normalizedSA-533 Grades B and CSA-662 Grade A

2 all materials of Curve B if produced to fine grainpractice and normalized and not listed for CurveD below

Figure 2-41 Dimensions of vessel used for MDMTexample

92 Pressure Vessel Design Manual

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 6: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

d Curve DSA-203SA-508 Class 1SA-516 if normalizedSA-524 Classes 1 and 2SA-537 Classes 1 2 and 3SA-612 if normalizedSA-622 if normalized

e For bolting the following impact test exemptiontemperature shall apply

f When no class or grade is shown all classes orgrades are included

g The following shall apply to all material assignmentnotes1 Cooling rates faster than those obtained by

cooling in air followed by tempering aspermitted by the material specification areconsidered to be equivalent to normalizing ornormalizing and tempering heat treatments

2 Fine grain practice is defined as the proceduresnecessary to obtain a fine austenitic grain size asdescribed in SA-20

Figure 2-42 Reduction in minimum design metaltemperature without impact testing

Figure 2-43 Impact test exemption curves

Spec No Grade

Impact Test Exemption

Temperature F

SA-193 B5 e20

SA-193 B7 e40SA-193 B7M e55

SA-193 B16 e20

SA-307 B e20

SA-320 B L7 L7A L7M L43 Impact tested

SA-325 1 2 e20

SA-354 BC 0

SA-354 BD thorn20

SA-449 e20SA-540 B2324 thorn10

General Design 93

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 7: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-44 Flow chart showing decision-making process to determine MDMT and impact-testing requirements

94 Pressure Vessel Design Manual

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 8: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Procedure 2-15 Buckling of Thin Wall Cylindrical Shells [21]

This section provides commentary on the buckling ofcylinders subject to external pressure uniform axialcompression a bending moment across the cross-sectionand in-plane shear stresses Cylinders may also be subjectto any combination of these loads Unstiffened or largering-stiffened cylinders may fail by local buckling orcolumn buckling and small ring-stiffened cylinders mayfail by local buckling column buckling general instabilityor local buckling of ring stiffeners The rings describedherein are assumed to be circumferential ring stiffenersThe terms lsquolargersquo and lsquosmallrsquo are consistent with Code Case2286 (and the incorporated Code Case 2286 methodologyin Section VIII Division 2 Part 4) where the term lsquolargersquorefers to a bulkhead where the number of circumferentiallobes is assumed to be two (n frac14 2) and the term lsquosmallrsquorefers to any larger number of circumferential lobes

Local buckling describes failure by buckling of thecylinder in a radial direction Column buckling for acylinder describes failure by out-of-plane buckling whilethe shape of the cross section prior to buckling is circularGeneral instability describes failure where one or morering stiffeners buckles along with the cylinder in acircumferential pattern with at least two waves Localbuckling of ring stiffeners refers to buckling of elementsof the ring stiffener

Note that an element in compression subject to1) elastic buckling will buckle before the element candevelop the yield stress 2) inelastic buckling will buckleafter some of the element develops the yield stress and3) plastic collapse will collapse after all of the elementdevelops the yield stress

External Pressure

Buckling of the cylinder due to external pressure mayoccur in the elastic inelastic or plastic range It isa function of Lrg and Dt ratios as well as the physicalproperties of the material Decreasing the effective lengthbelow the critical length has a positive effect the strengthof the cylinder under external pressure The critical lengthis the length at which the unstiffened cylinder

Decreasing the effective length may be done with ringstiffeners Where cylinders with lsquolargersquo stiffening rings areused the large rings will act as bulkheads whereby theshell portion between the rings acts similar to an unstiff-ened cylinder In this case the large rings are assumed notto buckle with the shell In general where cylinders with

lsquosmallrsquo stiffening rings are used the failure mode of generalinstability is introduced Specifically within the Code(Code Case 2286 and Section VIII Division 2 Part 4) thegeneral instability failure mode is precluded by increasingthe required moment of inertia of a small ring by a value of20 The difference between the large and small rings inCode Case 2286 is seen by using the more general equa-tion representing the small ring and using a value of nfrac14 2which yields the equation for the large ring Figure 2-45illustrates the meaning of circumferential buckling waveswhere the circle represents the original shape

Local buckling of ring stiffeners may be accomplishedby using compact shapes for ring elements Code Case2286 and Section VIII Division 2 Part 4 include geom-etry requirements (used from AISC) to ensure localbuckling of ring stiffeners is avoided

Axial Compression

Cylinders subject to uniform axial compression can failby global or local buckling in the elastic inelastic andplastic range Global buckling is usually determined by thelength to radius of gyration ratio (Lrg) and local bucklingis determined by the diameter to thickness ratio (Dt) Eachof these can be either elastic or inelastic In some casescircumferential ring stiffeners can be used on cylinders butthese are used mostly when external pressure is a concernThey may have a positive impact on axial compression ifthey are close enough to each other Code Case 2286 andSection VIII Division 2 Part 4 indicate that if the rings areless than 15(Rot)

12 from each other then the circumfer-ential rings are permitted to increase the calculated localbuckling strength due to axial compression and bendingLongitudinal or stringer stiffeners may be used toincrease the allowable axial capacity of the cylinderhowever these are not typically used in process plants andare more common in offshore platform supports

Cylinders under axial compression are more sensitive togeometric imperfections in the elastic range than in the

Figure 2-45 Circumferential buckling waves for n frac14 2(left) and n frac14 6 (right)

General Design 95

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 9: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

inelastic range For Code Case 2286 the reduction factorfor shape imperfections is 0207 for Dot values of greaterthan or equal to 1247 The factor becomes higher for lowerDot ratios The capacity reduction factors are already builtinto the allowable stress equations in Code Case 2286

Bending Moment

Cylinders subject to a bending moment across thecross-section have similar characteristics as the case ofa cylinder under uniform axial compression Ovaling ofthe cross-section occurs during bending however as out-lined in Code Case 2286 the allowable stress for a cylinderin bending is greater than a cylinder under uniform axialcompression for the same geometry

Shear

Cylinders subject to in-plane shear stresses can also failin the elastic inelastic and plastic range Though shearbuckling is rarely a controlling factor in the design of

process vessels the interaction may have an unfavorableeffect

Interaction

The effect of combining internalexternal pressure withaxial tensioncompression may be represented by anellipse created using a yield criterion In the four quadrantscreated by the yield criterion four combinations of theinternalexternal pressure with axial tensioncompressionmay be represented In the case of external pressurequadrants three and four (external pressure and axialcompression and external pressure and axial tension) arerepresentative of what is discussed here Furthermoreonly quadrant three is evaluated in Code Case 2286 andSection VIII Division 2 Part 4 since the topic of internalpressure is not addressed

Procedure 2-16 Optimum Vessel Proportions [16-20]

This procedure specifically addresses drums but can bemade applicable to any kind of vessel The basic questionis What vessel proportions usually expressed as LDratio will give the lowest weight for a given volume Themaximum volume for the least surface area and weight isof course a sphere Unfortunately spheres are generallymore expensive to build Thus spheres are not the mosteconomical option until you get to very large volumes andfor some process applications where that shape isrequired

For vessels without pressure atmospheric storagevessels for example the optimum LD ratio is 1 againusing the criteria for the maximum volume for theminimum surface area This optimum LD ratio varieswith the following parameters

PressureAllowable stressCorrosion allowanceJoint efficiency

In Process Equipment Design Brownell and Youngsuggest that for vessels less than 2 in in thickness theoptimum LD ratio is 6 and for greater thicknesses is 8However this does not account for the parameters just

shown Others have suggested a further breakdown bypressure categories

Although this refinement is an improvement it still doesnot factor in all of the variables But before describing theactual procedure a brief description of the sizing of drums ingeneral is warranted Here are some typical types of drums

Knock-out drumsAccumulator drumsSuction drumsLiquidndashvapor separatorsLiquidndashliquid separatorsStorage vesselsSurge drums

Typically the sizing of drums is related to a processconsideration such as liquid holdup (surge) storage

Pressure (PSIG) LD Ratio

0e250 3

250e500 4

gt500 5

96 Pressure Vessel Design Manual

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 10: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

volume or velocity considerations for separation Surgevolume in process units relates to the response timerequired for the alarms and operators to respond toupstream or downstream conditions

For small liquid holdup vessels tend to be verticalwhile for large surge volumes they tend to be horizontalFor small volumes of liquid it may be necessary toincrease the LD ratio beyond the optimum proportions toallow for adequate surge control Thus there may be aneconomic LD ratio for determining the least amount ofmetal for the given process conditions as well as a prac-tical operating LD ratio

For liquidndashvapor separators the diameter of the vessel isdetermined by the velocity of the product and the time ittakes for the separation to occur Baffles and demister padscan speed up the process In addition liquidndashvaporseparators must provide for minimum vapor spaces Thesizing of vessels is of course beyond this discussion and isthe subject of numerous articles

An economic LD ratio is between 1 and 10 LD ratiosgreater than 10 may produce the lowest surface-area-to-volume ratio but should be considered impractical formost applications Obviously plot space is also a consid-eration in ultimate cost In general the higher the pressurethe larger the ratio and the lower the pressure the lowerthe ratio As previously stated the optimum LD ratio foran atmospheric drum is 1 Average pressure vessels willrange between 3 and 5

Two procedures are included here and are calledMethod 1 and Method 2 The two procedures though

similar in execution yield different results Bothmethods take into account pressure corrosion jointefficiency and allowable stress Even with this muchdetail it is impossible to determine exactly whatproportions will yield the lowest overall cost sincethere are many more variables that enter into the ulti-mate cost of a vessel However determining the lowestweight is probably the best parameter in achieving thelowest cost

The procedure for determining the optimum LD ratiosfor the two methods is as follows

Given

V volumeP pressureC corrosion allowanceS allowable stressE joint efficiency

Method 1

1 Calculate F12 From Fig 2-46 using F1 and vessel volume V

determine the vessel diameter D3 Use D and V to calculate the required length L

Method 2

1 Calculate F22 From Fig 2-47 determine LD ratio3 From the LD ratio calculate the diameter D4 Use D and V to calculate the required length L

Table 2-8Optimum vessel proportionsdcomparison of two methods

V (cu ft) P (PSIG) Method1 D (ft) L (ft) t (in) W (lb) LD

1500 150 1 75 34 05625 20365 45

2 85 236 0625 20086 28

300 1 6 53 08125 35703 88

2 75 315 08125 28668 42

2000 150 1 7 52 05 25507 74

2 9 284 0625 24980 32

300 1 65 61 0875 51179 94

2 85 324 1125 39747 38

3000 150 1 85 53 0625 40106 63

2 105 311 06875 35537 3

300 1 75 68 09375 65975 91

2 95 392 125 69717 41

5000 150 1 10 64 06875 62513 64

2 115 443 1125 86781 39

300 1 85 88 1125 107861 104

2 115 443 1375 106067 39

1Methods are as follows based on graphs Method 1 K Abakians Hydrocarbon Processing June 1963 Method 2 SP Jawadekar Chemical

Engineering Dec 151980

General Design 97

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 11: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

98 Pressure Vessel Design Manual

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 12: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Atmospheric Tank Proportions

Table 2-9Optimum tank proportions

General Design 99

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 13: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-46 Method 1 Chart for determining optimum diameter

100 Pressure Vessel Design Manual

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 14: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-47 Method 2 Chart for determining the optimum LD ratio

GeneralDesign

101

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 15: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Procedure 2-17 Estimating Weights of Vessels and Vessel Components

Estimating of weights of vessels is an important aspectof vessel engineering In the conceptual phase of projectsweights are estimated in order to determine costs andbudgets for equipment foundations erection and trans-portation Estimated weights also help to get more accu-rate bids from suppliers Accurate weights are necessaryfor the design of the vessel itself to determine forces andmoments

There are a number of different types of weights thatare calculated Each weight is used for differentpurposes

1 Fabricated weight Total weight as fabricated in theshop

2 Shipping weight Fabrication weight plus anyweight added for shipping purposes such as ship-ping saddles

3 Erection weight Fabrication weight plus anyweight installed for the erection of the equipmentsuch as any insulation fireproofing piping laddersplatforms

4 Empty weight The overall weight of the vesselsitting on the foundation fully dressed waiting foroperating liquid

5 Operating weight Empty weight plus any operatingliquid weight

6 Test weight This weight can be either shop or fieldtest weight that is the vessel full of water

There are a number of ways to estimate the weights ofvessels depending on the accuracy required Vesselweights can be estimated based on computer designprograms These programs typically calculate the volumeof metal for the vessel shell and head and add weights forsupports nozzles trays and other components Anotherfast and easy way to get the volume of metal in the shelland heads is to use the surface area in square feet andmultiply this by the unit weight for the required thicknessin pounds per square foot

In addition to the base weight of metal in the shell andheads the designer must include an allowance for plateoverages per Table 2-11 The mill never rolls the plates theexact specified thickness since there would be the

possibility of being below thickness The safety marginadded by the mill is referred to as plate overage or over-weight percentage The plate overage varies by thethickness of the material

In addition to the plate overage the fabricator (or headmanufacturer) also adds a thinning allowance to the headto ensure that the head meets the minimum thickness in allareas Depending on the type of head the diameter andthe thickness required a thinning allowance can bedetermined This can be as much as 15 in for large-diameter hemi-heads over 4 in thick The metal does notdisappear during the forming process but may ldquoflowrdquo tothe areas of most work

On a typical spun 21 SE head the straight flange willget thicker and the knuckle will get thinner due to formingThe crown of the head should remain about the sameTherefore the completed head has a thickness averagingthe initial thickness of the material being formed

After the weights of all the components are added fora total weight an additional percentage is typically addedto allow for other components and welding The typicalpercentages are as follows

The weight of any individual component can easily becalculated based on the volume of the material times theunit density weight given in Table 2-11 Any shape canbe determined by calculating the surface area times thethickness times the density The designer need onlyremember the density of steel for most vessels of 02833lbin3 to determine any weight For vessels or compo-nents of other materials either the density of that materialor the factor for that material relative to carbon steel canbe used These values are also listed in the followingtables

lt50000 lb Add 1050000-75000 lb Add 8

75000-100000 lb Add 6

gt100000 lb Add 5

102 Pressure Vessel Design Manual

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 16: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 210General formulas for computing weights of vessel components

WEIGHT FORMULAS THICKNESS FORMULAS DATA

Per Ft 1068 Dm t ASME Section VIII Div 1 D = ID of shell or cone in

CS 89 Dm L t SHELL d = ID small end of cone in

Other π Dm L t δ Dm = Mean diameter of shell in

CS 89 Dm2 t t = Thickness in

Other π Dm2 t δ 21 SE HEAD Ac = Area of cone in2

CS 445 Dm2 t L = Length of shell or cone in

Other 157 Dm2 t δ δ = Density of material PCI

CS 307 Dm2 t HEMI HEAD R = Estimated radius of hemi head in

Other 1084 Dm2 t δ Ri = Inside radius in

CS 2833 Ac t S = Allowable stress PSI

Other Ac t δ P = Internal pressure PSIG CONE

t = (P Ri ) [Cos α (S E - 6 P )] E = Joint efficiency

ASME Section VIII Div 2 α = Half apex angle of cone degrees

SHELL FORMULAS

t = Ri (ePS - 1)Dm = D + tUse shell thickness in formula

HEMI HEAD R = 5 Dm - 25 t

For 30o cone Ac = 157 ( D2 -d2 )

For all other conesAc = π [5 (D + d) ] [L2 +(5 (D - d)2) ]12

t = (P Ri ) (S E - 2 P )

ITEM

SH

EL

L

t = (P Ri ) (S E - 6 P )

t = (P Ri ) (2 S E - 2 P )

t = Ri (e5PS - 1)

SP

HE

RE

HE

MI

21 S

E H

EA

DC

ON

E

NOTES

1 Add thinning allowance to all head thickness

General Design 103

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 17: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

104 Pressure Vessel Design Manual

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 18: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-11Weights of carbon steel plate and stainless steel sheet PSF

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

Thickness

(in)

Raw

Weight

Weight

Including

Overweight

Overweight

0125 51 565 1075 0875 357 3691 338

01875 766 834 9 09375 3828 3954 338

025 102 1097 75 1 408 4202 3

03125 1276 1361 675 10625 4338 4465 3

0375 153 1622 6 1125 4594 4728 3

04375 1786 1879 525 125 51 5253 3

05 204 2132 45 1375 5615 5778 3

05625 2297 2398 45 15 612 6304 3

0625 256 2646 375 1625 6635 6829 3

06875 2807 291 375 175 714 7354 3

075 306 3163 338 1875 7656 788 3

08125 3317 3427 338 2 816 8405 3

Stainless Steel Sheet

Thickness

Gauge

Weight Thickness Gauge Weight

10 GA 591 20 GA 158

11 GA 525 24 GA 105

12 GA 459 26 GA 0788

14 GA 328 28 GA 0656

16 GA 263 30 GA 0525

18 GA 21

Note Overweight is based on standard mill tolerance added to the thickness of plate to guarantee minimum thickness

General Design 105

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 19: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-12Weights of flanges 2 in to 24 in (lb)

106 Pressure Vessel Design Manual

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 20: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-13Dimensions and weights of large-diameter flanges 26 in to 60 in ASME B1647 Series B

General Design 107

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 21: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-14Weights of nozzles and manways 1 in to 60 in

108 Pressure Vessel Design Manual

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 22: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-15Weights of valve trays PSF

Dia

One Pass Two Pass Four Pass

CS Alloy CS Alloy CS Alloy

lt8400 13 11 14 12

8400 to 18000 12 10 13 11 15 13

gt18000 115 95 125 105 145 125

Notes

1 Compute area on total cross-sectional area of vessel The downcomer areas compensate for the weight of downcomers themselves

2 Tray weights include weights of trays and downcomers

Table 2-16Weights of tray supports and downcomer bars (lb)

ID (in) CS Alloy ID (in) CS Alloy ID (in) CS Alloy

30 25 17 102 113 72 174 287 174

36 28 19 108 119 75 180 294 178

42 34 23 114 123 77 186 344 207

48 37 25 120 176 108 192 354 212

54 44 35 126 183 112 198 362 218

60 47 38 132 188 116 204 374 226

66 50 40 138 195 119 210 385 231

72 53 44 144 202 122 216 396 239

78 55 46 150 244 149 222 407 245

84 99 62 156 251 152 228 418 252

90 103 65 162 271 162 234 428 259

96 109 68 168 278 167 240 440 265

Notes

1 Tray support weights include downcomer bolting bars as well

2 Tray support ring sizes are as follows

CS 1=200 2 1=200Alloy 5=1600 2 1=200

Table 2-17Thinning allowance for heads

Thickness

Diameter

lt15000 gt15000

012500 to 100 00625 None

100 to 200 0125 025

200 to 300 025 025

300 to 37500 0375 0375

37500 to 400 05 05

over 42500 075 075

General Design 109

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 23: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-18Weights of pipe (PLF)

Size

(in)

Schedule

10 20 30 STD 40 60 XS 80 100 120 140 160 XXS

075 08572 1131 1131 1474 1474 1937 2441

1 1404 1679 1679 2172 2172 2844 3659

125 1806 2273 2273 2997 2997 3765 5214

15 2085 2718 2718 3631 3631 4859 6408

2 2638 3653 3653 5022 5022 7444 9029

25 3531 5793 5793 7661 7661 1001 1369

3 4332 7576 7576 1025 1025 1432 1858

35 4973 9109 9109 125 125 1769 2285

4 5613 1079 1079 1266 1498 1498 19 2251 2754

5 777 1462 1462 2078 2078 2704 3296 3855

6 9289 1702 1897 1897 2857 2857 3639 453 5316

8 134 2236 247 2855 2855 3564 4339 4339 5087 6063 6776 7469 7242

10 182 2804 3424 4048 4048 5474 5474 6433 7693 892 1041 1156

12 242 3338 4377 4956 5352 7316 6542 8851 1072 1255 1397 1603

14 3671 4568 5457 5457 6337 8491 7209 1061 1307 1507 1702 1891

16 4205 5236 6258 6258 8277 1075 8277 1365 1648 1923 2235 2451

18 4739 5903 8206 7059 1046 1382 9345 1708 208 2441 2742 3085

20 5273 786 1041 786 1229 1664 1041 2089 2561 2964 3411 379

22 581 866 1148

24 6341 9462 1408 9462 1712 2381 1255 2964 3674 4294 4831 5419

26 1026 1362

28 1107 1468

30 989 1576 1961 1187 1576

32 1267 1682

34 1347 1789

36 1427 1896

42 1667 2216

110 Pressure Vessel Design Manual

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 24: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-19Weights of alloy stud bolts D (2) nuts per 100 pieces

Length

(in)

Stud Diameter in

05 0625 075 0875 1 1125 125 1375 15 1625 175 1875 2

3 29 49 76

325 30 51 79

35 31 53 82 120

375 32 55 85 124

4 34 57 88 128 188

425 35 59 91 132 194

45 36 61 94 136 199 246

475 37 63 97 140 205 253

5 39 65 100 144 210 259 330

525 40 67 103 148 216 266 338

55 41 69 106 152 221 272 347

575 71 109 156 227 279 355

6 73 112 160 232 285 363 460 568 700

625 115 164 238 292 371 470 580 714

65 118 168 243 298 380 480 592 728

675 172 249 305 388 490 604 742

7 176 254 311 396 500 616 756 900 1062 1227

725 260 318 404 510 628 770 916 1080 1248

75 265 324 413 520 640 784 932 1098 1270

775 271 331 421 530 652 798 948 1116 1291

8 276 337 429 540 664 812 964 1134 1312

825 344 437 550 676 826 980 1152 1334

85 350 446 560 688 840 996 1170 1355

875 357 454 570 700 854 1012 1188 1376

9 363 462 580 712 868 1028 1206 1398

925 370 470 590 724 882 1044 1224 1419

95 376 479 600 736 896 1060 1242 1440

975 383 487 610 748 910 1076 1260 1462

10 389 495 620 760 924 1092 1278 1483

1025 630 772 938 1108 1296 1508

105 640 784 952 1124 1314 1526

1075 650 796 966 1140 1332 1547

11 660 808 980 1156 1350 1569

1125 670 820 994 1172 1368 1590

115 680 832 1008 1188 1385 1611

1175 690 844 1022 1204 1404 1633

12 700 856 1036 1220 1422 1654

Add per

additional

1400 length

15 2 3 4 55 65 85 10 12 14 16 18 215

General Design 111

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 25: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-20Weights of saddles and baseplates (lb)

ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate ID (in)

Two CS

Saddles

12 3 6

Baseplate

34 3 8

Baseplate

24 100 70 150 138 3060 390 790

30 150 90 190 144 3400 410 820

36 260 105 215 150 3700 430 855

42 330 125 250 156 4000 450 885

48 380 140 285 162 4250 460 920

54 440 160 320 168 4500 480 950

60 510 170 350 174 4750 490 985

66 590 190 385 180 5000 510 1020

72 680 200 420 186 5250 530 1050

78 910 220 450 192 5500 540 1080

84 1050 240 485 198 5750 560 1120

90 1160 260 520 204 6000 580 1150

96 1230 280 550 210 6250 590 1190

102 1730 290 585 216 6500 610 1220

108 1870 310 615 222 6750 630 1250

114 2330 330 650 228 7000 650 1290

120 2440 340 690 238 7250 660 1320

126 2700 360 720 240 7500 680 1360

132 2880 380 755

Table 2-21Density of various materials

Material d (lbin3) PCF Weight Relative to CS

Steel 02833 490 100

300 SST 0286 494 102

400 SST 0283 489 099

Nickel 200 0321 555 113

Permanickel 300 0316 546 112

Monel 400 0319 551 113

Monel 500 0306 529 108

Inconel 600 0304 525 107

lnconel 625 0305 527 108

Incoloy 800 0287 496 101

lncoloy 825 0294 508 104

Hastelloy C4 0312 539 110

Hastelloy G30 0297 513 105

Aluminum 0098 165 035

Brass 0297 513 105

Cast iron 0258 446 091

Ductile iron 0278 480 098

Copper 0322 556 114

Bronze 0319 552 113

112 Pressure Vessel Design Manual

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 26: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

SIZE

BO T Y C N d G E R F H WT

14 34 75 1875 27 16 275 1406 263 338 2025 11 1750

16 38 775 195 30 16 3 1593 288 363 2275 115 2250

18 41 825 205 34 20 3 1781 288 363 2675 12 2850

20 45 85 22 3925 24 3 193 288 363 32 1325 3800

24 52 95 24 45 20 35 234 35 4 37 1425 5500

2 ASME B165 dimensions for 2500 flanges stopat 12 NPS These dimensions should be consideredan extension of the B165 size range

SPECIAL DESIGN RFWN FLANGES FOR CLASS 2500

3 These dimensions can be used as a starting placefor special designed flanges

Notes

1 These dimensions and weights should be used forestimating purposes only

Dimensions for Weld Neck Flange

PIPE

FLANGE

BOLT

B

GASKET

F

C

Gd

T

HYRING HUB

ER

O

General Design 113

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 27: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

SIZE RATING B O WN

Wb

WS

Wf

Wp

WT

518140703233400603011539092855009096137181705888005107035416325201526100525601779859233500652410112213145170090003461203577386100510034083845003159910052053111161187313600607717817514947180095763372383579929100515747085087006100420052

WEIGHTS OF QUENCH NOZZLES

10 X 4

12 X 6

9

11

14 X 8

10

12

14

1) 600 amp 900 assumes Type HB Conn

2) 1500 amp 2500 assumes Type F Conn

DATA

WN = Weight Nozzle Lbs

Wb = Weight Blind Lbs

135

39

70

115

Wp = Weight Internal Pipe and Flange Lbs

WT = Weight Total Lbs

B = Bore of Vessel Nozzle In

NOTES

Ws = Weight Studs amp Nuts for Blind Lbs

O = OD of Internal Flange In

3) Wp assumes weight of 12 of Sch 160 Pipe and the 150 internal flange

Wf = Weight Flange Lbs

REACTOR SHELL (Cr-Mo)

VESSEL NOZZLE (Cr-Mo)

BLIND FLG (Cr-Mo)

PIPE amp FLG (Cr-Mo)

WELD OVERLAY

WELD OVERLAY

150 WELD NECKOR SLIP ON FLG

SOLID SST

CL

114 Pressure Vessel Design Manual

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 28: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

DIA RATING A B C D θ WEIGHT DIA RATING A B C D θ WEIGHT

578006578006

03010090301009

0621005106210051

5281005252810052

588006529006

04010090801009

0721005101310051

0381005257810052

528006058006

0890090001009

0121005153210051

5771005200810052

048006077006

0401009029009

0721005155110051

5381005251710052

078006

5701009

05210051

51810052

188 144

3 Dimensions are in Inches weights in Lbs

82 40

0429533762193188 121

92 35

231271111537802164148

169 138

101 176 144

NOTES

1 Weights amp dimensions are for estimating purposes only

2 Dimensions are based on 8 nozzle

69031902193196 13

14

15

16

30

10

11

12 92 161 132 89 35

DIMENSIONSWEIGHTS OF BOTTOM CATALYST DUMP NOZZLES

8

9

91 35

76 152 132 98

BA

TL

C

DBOSS

HEMI HEAD

PIPE8rdquo SCH 160

FLANGE

BLIND

STUDSNUTS

θ

General Design 115

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 29: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

N d L

24 600 37 24 33 30 2825 213 18 4 24 1875 1325 2725 1500 37024 900 41 24 355 3162 295 3188 20 55 20 25 175 2725 2160 71524 1500 46 24 39 3362 30 5563 22 8 16 35 245 2725 3400 155024 2500 52 24 45 45 395 65 24 95 20 35 275 2725 6000 2110

30 600 48 30 4025 43 3394 9 24 463 28 2 1475 3613 1600 53530 900 50 30 43 445 3575 1044 26 656 20 25 1962 365 3400 77030 1500 52 30 4475 46 375 1263 28 8 24 25 225 3925 5500 102530 2500 58 30 52 50 4588 531 30 95 24 3 265 3975 12000 1730

36 600 52 36 475 47 44 4 29 488 28 225 1575 4025 2500 73036 900 54 36 51 51 4563 644 31 675 20 35 22 4025 3800 182036 1500 56 36 50 53 46 625 33 825 28 25 23 4425 10660 111536 2500 62 36 56 5438 5138 475 36 95 28 3 265 4425 15000 2020

L = 2 T + 2 d + 15

a = Width of Raised Face in = Gasket Width + 5 Min

2) All flange designs shown are non-standard except for the 24 600 thru 1500 only3) All flange designs based on 2-14 Cr - 1 Mo material at 850 deg F

WS

Notes

T

Studs

E F

A = C + 2 d

R

1) These dimensions and weights should be used for estimating purposes only Detail designs have not been calculated

HCBAeziS moN WND

L = Length of Studs in

C = Bolt Circle in

WN = Weight Nozzle Lbs

WS = Weight Studs amp Nuts LbsX = Width across Flats of Nuts inR = B + 2a

F = f + (D - E)2

h = H - T - F -25

BS = Min Bolt Spacing = 21 d

Table of Dimensions and Weights for Large Diameter Self-Reinforced Manways

ataDsalumroF

N = Qty Studsd = Dia Studs inf = d + 25

C = A - 2 d Min = (BS N) π

E = C - X

D

E

RCAASSUME

RF14 Prime

Hh

fTF

B

ss

116

Pressure

VesselDesignManual

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 30: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

SIZE RATING T WB SIZE RATING Wf SIZE b Wp We

600 4 1175 600 226 8 12 75 117

900 55 2080 900 372 10 15 160 226

1500 75 3500 1500 670 12 18 200 300

2500 95 5580 2500 800 14 21 250 410

600 463 2080 600 334 16 24 300 530

900 656 3725 900 562 18 27 350 675

1500 8 5000 1500 940 20 30 400 840

2500 105 7140 2500 1750

600 488 3300 600 462

900 675 5700 900 685

1500 825 5400 1500 940

2500 1225 9700 2500 2260

600 531

SIZE RATING Wf 900 924

52610051081006

05820052862009

8760064540051

461100957010052

1500 2050

2500 3800

NOZZLE FLANGE

10

18

20

3 Weld neck is included in blind flg weight

4 Studs and nuts are not included

DATA

WB = Weight Blind Lbs

Wf = Weight Outlet Flange Lbs

We = Weight Elbow Lbs

Wp = Weight Pipe Lbs

WT = Weight Total

WT = WB + Wf + We + Wp

24

30

36

12

14

16

REACTOR INLET ESTIMATED WEIGHTS

NOTES

1 Dim B = T + b + 6

2 Pipe amp elbow assumed as Sch 160

PIPE amp ELBOWDNILB

VARIES

BASSUME 12

ASSUME 6 ASSUME14 RF

WELD NECKWB

We

Wp

Wf

T

b

LIFTING LUG

NOZZLE FLANGE

General Design 117

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 31: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

We

Wf

Wb

Wp

WT

6 69 675 4625 53 164 90 198 505

8 72 838 4163 117 273 150 300 840

10 75 10 37 226 454 232 416 1330

6 75 675 5225 53 164 90 220 527

8 78 838 4763 117 273 150 335 875

10 81 10 43 226 454 232 475 1390

10 83 838 49 226 454 232 550 1470

12 86 10 4488 375 670 320 705 2070

d = Nominal pipe Size in 14 89 1113 4125 570 940 380 780 2670

Wb = Weight Boss Lbs 10 92 838 55 226 454 232 610 1520

We = Weight Elbow Lbs 12 95 10 5088 375 670 320 785 2150

Wp = Weight Pipe Lbs 14 98 1113 4725 570 940 380 875 2765

Wf = Weight Flange Lbs 12 100 838 5888 375 670 320 920 2285

WT = Weight Total 14 103 10 5525 570 940 380 1035 2925

WT = Wb + We + Wp + Wf16 106 1113 5175 800 1250 490 1260 3800

12 109 10 6488 375 670 320 1000 2365

14 112 1113 6125 570 940 380 1130 3020

Bmin = 5 D + 15 d + Lp1 + 6 16 115 1175 5775 800 1250 490 1385 3925

14 120 1113 6725 570 940 380 1255 3145

16 123 1175 6375 800 1250 490 1547 4087

Lp2 = A - 15 d - Y 18 126 1225 6012 1200 1625 620 1860 5300

14 129 1175 7325 570 940 380 1350 3240

16 132 1225 6975 800 1250 490 1670 4210

55450102026526100213166882153181061 hcS sa demussa era woblE ampepiP 1

0734038109405210085757522104161 0051 sa demussa si egnalF 2

18 143 1288 7213 1200 1625 620 2220 5665

in

62

REACTOR BOTTOM OUTLET ESTIMATED WEIGHTS

WEIGHTS (Lbs)DIA

Ft

d

in

A

in

B

in

Y

in

Lp1

Lp2

in

EQUATIONS

DATA

8

9

14

15

16

10

11

12

13

14

Amin = 8 to 115 Dia 5D + 1412 to 16 Dia 5D + 16

NOTES

68

74

80

88

94

100

106

112

6

6

8

8

10

10

12

12

20 146 14 68 1650 2050 760 2590 7050

B

YA

Wb

We

WpWf

TAN LINE

SKIR

TLp1

Lp2

Hemi-head

118

Pressure

VesselDesignManual

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 32: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

1010

SIZE RATING A B C D e f g h b a P T WEIGHT

058521252815521862350289294141889622006

540183428231644131735222336615101152009

1500 282 1031 155 18 36 25 4238 162 748 32 35 1300

2500 322 1138 19 214 429 27 4862 225 1031 36 45 2320

600 355 1194 165 167 334 36 4884 138 584 42 2438 1800

900 384 1244 185 19 38 38 5366 163 716 45 275 2530

1500 406 1294 19 204 408 40 5843 188 853 48 388 2960

2500 445 1412 2175 234 468 42 6438 225 1107 52 525 4425

00435725556515168483910251654006

0034385657816605424212512551684009

e = 707 D + ts

5 There is no weight allowance for the shell portion of the nozzle

FORMULAS

4 Shell thickness assumed as follows 600 = 5 900 = 61500 = 7 2500 = 8

a = T + b + 5 (D - C)

h = g + a + 1414 ts

f = 2 e

6

8

DIMENSIONS amp WEIGHTS OF SIDE CATALYST DUMP NOZZLES

6

8

NOTES

1 Weights amp dimensions are for estimating only

2 Dimensions are in inches

3 Weights are in Lbs

A = 707 P + 354 D

074554263892251725864432326061250051

2500 575 1738 265 267 534 54 79 275 1381 68 675 8030

10

hg

BD

C

bT

REMOVABLEPLUG

k

e Pef

t

ww

w

w

s

fN

B

b

a

A

45deg

GeneralDesign

119

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 33: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-22Weight of (1) hemispherical head based on inside diameter LBS

Specified

Min Thk

ts (in)

Thk w

thinning

allowance

Ta

Diameter in

24 36 48 60 72 84 96 108 120 132 144 156 168 180 192 204

0380 0560 151 334 590 918 1318 1790 2334 2950 3638

0500 0690 186 412 725 1126 1616 2194 2860 3614 4456

0630 0810 223 490 861 1337 1917 2600 3388 4281 5277 6377 7582 8890

0750 0940 260 570 1000 1550 2220 3010 3920 4950 6100 7373 8763 10275

0880 1060 297 650 1138 1763 2524 3421 4454 5624 6930 8371 9950 11664 13514

1000 1190 335 730 1279 1978 2830 3835 4991 6300 7760 9374 11140 13056 15126

1130 1500 434 938 1635 2524 3606 4880 6345 8000 9854 11900 14131 16558 19177 21989 24992 28189

1250 1630 475 1024 1780 2746 3920 5300 6892 8690 10697 12912 15335 17966 20806 23855 27110 30575

1380 1750 516 1110 1927 2970 4236 5726 7441 9380 11543 13931 16543 19380 22440 25725 29233 32967

1500 1880 559 1197 2075 3194 4558 6153 7992 10073 12393 14954 17755 20796 24078 27600 31362 35365

1630 2000 602 1285 2225 3421 4874 6582 8547 10769 13247 15980 18971 22218 25721 29480 33500 37770

1750 2130 645 1375 2375 3650 5195 7014 9105 11468 14104 17011 20191 23644 27370 31365 35635 40177

1880 2250 690 1465 2528 3880 5520 7450 9665 12170 14964 18045 21415 25075 29021 33256 37780 42592

2000 2380 735 1556 2682 4112 5846 7885 10228 12875 15827 19083 22645 26510 30679 35152 39930 45013

2130 2750 3150 4818 6838 9209 11933 15010 18440 22220 26354 30840 35679 40870 46413 52310

2250 2880 3311 5057 7172 9655 12508 15728 19316 23273 27600 32293 37355 42786 48586 53242

2380 3000 5300 7510 10105 13084 16450 20650 24330 28850 33750 39914 44708 50763 57203

2500 3130 5540 7850 10555 13664 17173 21082 25391 30100 35210 40722 46634 52946 59660

2630 3250 8190 11010 14246 17900 21969 26455 31358 36678 42414 48566 55135 62120

2750 3380 8532 11465 14831 18630 22860 27524 32620 38148 44109 50500 57330 64587

2880 3500 11925 15240 19365 23755 28600 33885 39625 45810 52445 59530 67060

3000 3750 12850 16605 20840 25555 30750 36430 42590 49225 56345 63945 72025

3250 4000 17800 22330 27370 32925 38990 45570 52660 60265 68380 77010

3500 4250 19000 23830 29200 35110 41570 48570 56115 64200 72840 82020

3750 4500 20225 25345 31040 37310 44160 51585 59590 68165 77320 87050

4000 5000 22700 28400 34765 41760 49400 57675 66600 76150 86350 97190

4250 5250 29960 36650 44000 52040 60750 70125 80175 90900 102300

4500 6000 34700 42400 50850 60075 70000 80840 92370 104675 117750

5000 6500 46286 55485 65516 76380 88077 100607 113971 128167

5250 7000 50242 60185 71025 82762 95400 108928 123357 138683

5500 7250 52241 62558 73805 85982 99086 113121 128084 143976

5750 7750 67355 79418 92475 106525 121570 137605 154635

6000 8000 69775 82250 95750 110275 125825 142400 160000

Notes

1 Assumes carbon steel material (unit wt frac14 2833 PCI)

2 Thinning allowance Ta per Table

3 Formulas are as follows W frac14 445 Dm2 t Dm frac14 D thorn t and t frac14 ts thorn Ta

Table 2-23Thinning allowance for hemi-heads

Thickness (in) Thinning Allowance Ta

0125 to 1 019

1 to 2 038

2 to 3 063

3 to 375 075

4 to 45 1

45 to 5 15

5 to 55 175

575 to 6 2

120 Pressure Vessel Design Manual

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 34: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

General Design 121

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 35: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

122 Pressure Vessel Design Manual

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 36: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

General Design 123

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 37: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Procedure 2-18 Design of Jacketed Vessels

External jackets are used to heat or cool the contents ofa vessel In effect this turns the pressure vessel into a heatexchanger Jacketing is an optimum means to accomplishthis in terms of control efficiency and product qualityThe advantages are as follows

1 All liquids can be used Steam is ideal for heatingWater or Glycol are ideal for cooling

2 Circulation temperature and velocity of the heatingcooling media can be carefully controlled

3 Jackets may be fabricated from a much less expen-sive metal than the shell

4 Cleaning and maintenance can be minimizedproviding a ldquocleanrdquo media is utilized

Jackets are frequently used in combination with internalheating coils or agitators Jacketed vessels are much morecommon in the food beverage and chemical industry thenin the refining industry The applications are limited in therefining industry because the services in refining appli-cation tend to be fouling and not clean Most refineryapplications for heat exchange are dirty services andtherefore must be capable of being taken apart for clean-ing Since a jacketed vessel can only be cleaned withsteam or chemicals it is not considered practical for mostrefinery services

The types of jackets used on vessels are as follows

1 Conventional (AKA ldquoPlainrdquo)2 Jacket with a spiral baffle3 Spiral pipe coil welded to the shell4 Spiral half pipe coil welded to the shell5 Dimpled jacket

Conventional Jacket

Used with steam or cooling Liquid flow velocities arelow and the flow is poorly distributed Natural convectionequations are suitable and cooling coefficients have lowvalues Conventional jackets are best applied to smallvessels or high pressure applications where the vesselinternal pressure is twice the jacket pressure asa minimum The conventional jacket is the most common

type An often used variation of this configuration is madeby dividing the straight side into two or more separatejackets

Jacket with a Spiral baffle

This design is a variation of the conventional jacketThe internal spiral baffle allows for high flow velocities tobe reached Some clearance must be allowed for betweenthe baffles and the inside of the jacket to allow forassembly fabrication and tolerances Although thisclearance may be small the total leakage area per baffleturn may be substantial when compared with the crosssectional flow area of the baffle passage Thus the actualvelocity may only be a fraction of the calculated value Tocompensate for this leakage around the baffles it is rec-ommended that a 10 allowance be applied to either thetotal area required or total heat required

Spiral Pipe Coil Welded to the Shell

This design is not used frequently due to the minimalcontact area between the shell and coil It does howeveralleviate one of the problems of constructing a half-pipecoil That is the cutting of the coils in half and thesubsequent wastage Some techniques have been devel-oped to form flat strips into half pipe coils to save wastageand labor There is just as much welding required forattaching a full pipe coil as there is with the half pipe

Spiral Half Pipe Coil welded to the shell

This design provides high velocity and turbulencewithin the jacket This in turn will result in an unusuallyhigh film coefficient The half pipe coil is recommendedfor high temperature and all liquid applications It is betterthan conventional jackets because the pressure drop canbe carefully controlled and calculated It is not howeverpractical for small vessels less than 500 gallons Becausethere are no limitations to the number of inlet and outletconnections this type of jacketing can be divided intomultiple zones for maximum flexibility and efficiency

124 Pressure Vessel Design Manual

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 38: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

For maximum heat transfer the coils should be spacedabout frac34rdquo (19mm) apart but other spacing is aceptableStandard sizes are 2rdquo 3rdquo or 4rdquo NPS

Dimpled Jackets

There are two main types of dimpled jackets These are

1 Integral construction2 Bolted-on or clamp-on type

The bolted-on types are less expensive but do not havecompletely reliable heat transfer characteristics due to theldquofitrdquo of the clamp-on sections Sometimes a heat transfermastic is used between the two surfaces Advantages areas follows

1 They are cheap2 They are completely replaceable3 The service can be easily altered4 The shape and configuration can be easily modified5 They do not exert any external pressure on the

vessel shell

The integral type utilizes the inner surface of the dimplejacket for the vessel shell Advantages of the integral typeare as follows

1 They are cheaper than a conventional jacket2 The savings increase with higher pressures and

larger vessels3 They are cheaper than the half pipe jacket for low

internal pressures

General

External Pressure

The inner vessel shall be designed to resist the maximumdifferential pressure Typically this would be the designpressure of the jacket The differential pressure shouldinclude accidental vacuum in the inner vessel Particularattention should be given to the effects of local loads anddifferential expansion

The spiral baffles may not be considered as contrib-uting stiffness to the shell for the case of external pressuresince they are not closed circumferential rings If stiff-ening rings are required they must be placed inside thevessel This may be a problem from a process standpointThe alternatives are to increase the shell thickness or

shorten the jacket into smaller sections to reduce the Ldimension

Per ASME Code if the internal pressure is greater than167 times the external pressure the external pressure willnot govern

The half pipe coil causes an external pressure on thevessel shell but only inside the coil area and then not ina complete 360 circumferential zone Therefore theeffects on the vessel shell are negligible

Design

There are two distinct aspects of the design of jacketsfor heat transfer These are the thermal design and thephysical design The thermal design falls into threeparts

1 Determine the proper design basisa Vessel proportionsb Maximum depth of liquidc Time required to heatcoold Agitated or non-agitatede Type of operation batch or continuous

2 Calculating the required heat load3 Computing the required surface area

Physical design includes the following

1 Selecting the type of jacket2 Determine the areas of the vessel shell to be heated

or cooled3 Determine whether external connections are

a Separateb Seriesc Parallel

4 Determine pressure drop

The type of operation is characterized in the followingcases

1 Batch operation Heating2 Batch operation Cooling3 Continuous operation Heating4 Continuous operation Cooling

Pressure Drop

It is important that pressure drop be considered inthe design of an external jacket This will establish thepractical limits on the length of passageway inside thejacket

General Design 125

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 39: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Pressure drop in conventional jackets without spiralbaffles and dimple jackets are deliberately excluded fromthis procedure Other sources should be consulted forthese applications

For design purposes the half pipe coil and conventionaljackets with spiral baffles are treated as coils Thisprocedure converts the shape of the passageway into anequivalent diameter pipe coil

Large pressure drops may mean the passageway is notcapable of transmitting the required quantity of liquid atthe available pressure In addition the fluid velocitiesinside the passageway should be kept as high as possibleto reduce film buildup

There are no set rules or parameters for maximumallowable pressure drop Rather an acceptable pressuredrop is related to the velocity required to effect theheat transfer For liquids a minimum velocity of 1 to 3feet per second should be considered as minimum Forgases ldquorho V squaredrdquo should be maintained around4000

Pressure drop in spiral passageways is dependent onwhether the flow is laminar or turbulent Typically flowsare laminar at low fluid velocities and turbulent at highfluid velocities In spiral passageways a secondary circu-lation takes place called the ldquoDouble Eddyrdquo or ldquoDeanEffectrdquo While this circulation increases the friction loss italso tends to stabilize laminar flow thus increasing theldquocriticalrdquo Reynolds number

In general flows are laminar at Reynolds numbersless than 2000 and turbulent when greater than 4000At Reynolds numbers between 2000 and 4000 inter-mittent conditions exist that are called the ldquocriticalzonerdquo

For steam flow the pressure drop will be high nearthe inlet and decrease approximately as the square ofthe velocity From this relationship combined with theeffects of increased specific volume of the steamdue to pressure drop it can be shown that theaverage velocity of the steam in the coil is frac34 of themaximum inlet velocity For the purposes of calculatingpressure drop this ratio may be used to determine theaverage quantity of steam flowing within the spiralpassageway

In cases where a high velocity is required in order toutilize a high heat transfer coefficient the pressure dropbecomes important If the pressure drop exceeds thepressure output of a positive displacement pump then

there is a real possibility that the pressure of the jacket willexceed the design conditions

In the case of a centrifugal pump the velocity of thefluid will adjust to the pump pressure available Thismay result in a lower heat transfer coefficient thenrequired

For either a dimple jacket design or a half pipe jacketthe pressure drop will be higher than that of an equiv-alent conventional jacket due to the increasedturbulence

The preferred method to reduce pressure drop is toshorten the path of the fluid and manifold the inlets andoutlets by ldquoparallelrdquo routing The ldquoseriesrdquo type externalpiping connections will increase the overall pressure dropSee Figure 2-50

Heat Transfer Coefficient U

The Heat Transfer Coefficient U is dependent on thefollowing variables

1 Thermal conductivity of metal medium and product2 Thickness of metal in vessel shell3 Fluid velocity4 Specific heat5 Density and viscosity6 Fouling factor (oxidation scaling)7 Temperature differences (driving force)8 Trapped gasses in liquid flow9 Type of flow regime (laminar versus turbulent

turbulent being better)

Agitation

In order to effect the best heat transfer possible it ispreferable to have the contents circulated with an agitatoror mixer This is desirable but not mandatory

In many cases agitators are provided as part of theprocess for blending or mixing not purely to enhance heattransfer

However there is a ldquonatural circulationrdquo set up by theheating of a product inside a vessel that will occur Thiscirculation is driven by the warmer product rising in thetank

Agitation will also help to prevent buildup or fouling ofthe vessel wall This provides for the use of a higher heattransfer coefficient

126 Pressure Vessel Design Manual

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 40: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Notation

AC frac14 Cross sectional area of jacket flow area in2

Ar frac14 Cross sectional area of jacket flow area in2

D frac14 Vessel OD FtDe de frac14 Equivalent inside diameter of passageway De

is in Ft de is inchesf frac14 Friction factor

FLF frac14 Laminar flow factorg frac14 Acceleration due to gravityfrac14417 108

FtHr2

j frac14 Jacket width inL frac14 Design length of jacket section inLP frac14 Length of path of travel Ft

LBP frac14 Baffle pitch inM frac14 Mass flow rate LbsHrN frac14 Number of turns of spiral baffle or half pipeP frac14 Internal design pressure in jacket PSIp frac14 Pitch of half pipe coil inQ frac14 Total heat required BTUHrQL frac14 Heat loss from the exterior of the vessel shell

and jacket BTUHr

r frac14 Radius of toroidal section of closure inRe frac14 Reynolds numberRec frac14 Critical Reynolds numberRi frac14 Inside radius of vessel inRj frac14 Inside radius of jacket inRS frac14 Outside radius of vessel inS frac14 ASME Code allowable stress tension PSItC frac14 Thickness of closure bar intj frac14 Thickness of jacket intrJ frac14 Thickness required jacket intrC frac14 Thickness required closure bar intS frac14 Thickness of vessel shell inU frac14 Heat transfer coefficient BTUHrFt2FV frac14 Velocity of media FPS or FPHW frac14 Rate of flow in jacket LbsHr

Y Z frac14 Weld sizes inr frac14 Density of fluid PCF

DP frac14 Pressure drop PSIDPL frac14 Straight line pressure drop PSI

m frac14 Dynamic viscosity cP

(a) (b)

(c) (d) (e)

Space

Figure 2-48 Types of Jacket Construction (a) Plain Jacket (b) Jacket with Spiral Baffle (c) Pipe Coil Welded to Shell(d) Half-Pipe Welded to Shell (e) Dimpled Jacket

General Design 127

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 41: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-49 Some acceptable types of jacketed vessels

128 Pressure Vessel Design Manual

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 42: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-50 External piping configurations for multi-jacketed vessles GeneralDesign

129

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 43: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Figure 2-51 Miscellaneous jacket details

130 Pressure Vessel Design Manual

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 44: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Types 2 and 4 Jackets

30 deg max

Min throat dimension = t

c

θ max = 60 deg

07Y min

07Y min

07Y min

07Y min

07Y min

07Y min

d-1

e-2 f-1

d-2

Y

Y

Y

Y

Y

Y

Y

Y

Y

c

Y

Y

Y

07Z minZ

Z

Z

Z

Z

Y

Z

Z

Z

07Y min

07Y minY

Type 1 Jackets

Min 2tc but need

not exceedfrac12 in (13 mm)

Y = 07tc

a-1

b-1 b-2 b-3

15tc

tc min t

c min

(Elongated tomaintain minthroat dimension)

tc

tc

tc

tc t

cts

j

Rs

Rj

tj

ts j

Rs

Rj

tj

ts

j

Rs

Rj

tj

r

r min = 3tc

083tc min

125tc min 125t

c min

tc min

tc min

125tc min

a-2 a-3

r min = j r min

= 2tc

See Note (1)

tc

tc

See Note (1)

ts j

Rs

Rj

tj

r min = 3tc

See Note (1)

ts

ts

j j

Rs

Rs

Rj

Rj

Rs

Rj R

s Rj

tj

tj

ts

j tj

tc

Y

tc

07Z min

tc

tc

ts j t

j

ts

ts

j tj

e-1

See Note (1)

Y = a + b

Rs

Rs

Rj

Z

Z

a

b

θ max = 30 deg

Figure 2-52a Some acceptable types of jacket closures

General Design 131

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 45: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Y = a + b

Y = a + b

Z

Z

ZZ

Z

Z

a

a

b

b

Z

Z

tc

tc

tc

tc

tj

tj

ts

Rs

Rs

ts

f-2

g-3 g-4 g-5

f-3 g-1 g-2

tjmin

Rj

Rj

See Note (1)

45 degmin

Weld detail perFig UW-132 (c)

Weld detail perFig UW-132 (d)

See Note (1)

Plug weldper UW-17

See welding details[sketches (i-1) and (i-2)]

Torispherical ellipsoidal and hemisphericalheads (OD of jacket head not greater than ODof vessel head or ID of jacket headnominally equal to OD of vessel head)

See details[sketches (f-1) to (f-3)and (g-1) to (g-6)]

Weld detail perFig UW-132(e)

tj

tj

2tj min

07tj min

083tj min

tj min

tj

Rj

15tj

(Elongated to maintain min throat dimension)

tj min

Rj R

j

tc

Not lessthan a

atc t

c

g-6

tj

Rj

30 deg max

tj min

Min throat dimension = tj

tc

A gt B A = B A lt B Conical and Toriconical

i-1 i-2 i-3 k

h

I

t3

tj = ⅝ in

(16 mm) max

tj = ⅝ in

(16 mm) max

A

t3

A

B B

See Note See Note

tj = ⅝ in

(16 mm) max

t3

tj max

Z = 083tj min

Y = 15tj min

A

B

Figure 2-52b Some acceptable types of jacket closures (Continued)

132 Pressure Vessel Design Manual

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 46: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-24Notes To Figure 2-52

Fig NotesRemarks Fig NotesRemarks

a-1 a Type 1 jacket only f-1 f-2 amp f-3 a May be used for any type jacket

b trc trj b For Type 1 jacket the closure bar thk shall be

the greater of the following

c r 3 tc 1 trc frac14 2 trj

d trc frac14 625 (16 mm) max 2 trc frac14 707 J (P S )12

e Y 7 tc c For all other jacket types

a-2 amp a-3 a Type 2 or 4 jackets only trc frac14 1414 [(P RsJ) S)12]

b trc trj J frac14 [(2 S ts2)(P Rj)] - 5 (ts thorn tj )

c r 3tc d Weld sizes

d trc frac14 625 (16 mm) max Y Smaller of 15 tc or 15 tse Y 83 tc

b-1 amp b-2 a trc trj where Y frac14 Sum of a thorn b

b-3 a trc trj Z frac14 Min fillet weld size used to maintain the

min Y dimension

b trc 707 J (P S )12 g-1 g-2 amp g-3 a May be used with any type jacket

c a Type 1 jacket only

b q frac14 30 max g-4 g-5 amp g-6 a May be used with any type jacket

c trc frac14 (P r) [cos q

(SE - 6 P)]

b trc frac14 625 (16 mm) max

d trc trj h a Type 3 jacket only

d-1 d-2 e-1 amp e-2 a Type 1 jacket only b Attachment welds shall be in accordance with

Figures i-1 i-2 or i-3b trj frac14 625 (16 mm) max

c Min thk of closure bar shall be

the greater of the following

c trj frac14 625 (16 mm) max

1 trc frac14 2 trj i-1 i-2 amp i-3 a Weld details for jackets attahed to heads

2 trc frac14 707 J (P S )12

d Y Smaller of 75 tc or 75 ts k or l a Closures for conical or toriconical closures only

e Z tj b Type 2 jacket only

Note 1

For sketches b-1 b-2 b-3 e-2 g-2 and g-3 a backing strip may be used with a full penetration weld

General Design 133

Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

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Procedure 2-19 Forming StrainsFiber Elongation

Nomenclature

d frac14 Original ID of pipe or tube indf frac14 Final OD of pipe or tube indo frac14 OD of pipe or tube inD frac14 Finished ID of pipe or tube inDb frac14 Diameter of blank plate or intermediate product

inDf frac14 Final OD of pipe or tube inDo frac14 Original OD of head inFE frac14 Fiber elongation L1 frac14 Developed length of two knuckles of head or

cone inL2 frac14 Developed length of crown of head or hemi-

sphere inL frac14 Initial length of swaged or flared section of pipe

or tube inLf frac14 Final length of swaged or flared section of pipe or

tube inro frac14 Outside radius of pipe or tube inRc frac14 Centerline bend radius of pipe or tube inRf frac14 Final mean radius inRo frac14 Original mean radius of plate for head Assume

Nif forming begins with a flat platet frac14 Thickness of plate in

tA frac14 Wall thickness of pipe or tube before bending orforming in

tB frac14 Wall thickness of pipe or tube after forming inεf frac14 Forming strain or fiber elongation

Expected Wall Thinning of Pipe Bends

tB frac14 frac12 Rc=ethRc thorn 5 doTHORN ethtATHORNRf frac14 Rc thorn ro 5 tB

Blank Diameter for Formed Heads (Developed Length)

Dimensions

a frac14 5ethDm 2 rTHORNSin a frac14 a=ethL rTHORNa frac14b frac14 90 a

bull Length of knuckles L1

L1 frac14 2rb ethp=180THORNbull Length of crown L2

L2 frac14 2La ethp=180THORNbull Diameter of blank necessary Db (developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

Assumes 1 in for machining

Example 1 Formed Head

Given 100 in ID 21 SE Head 1 in thick

Dm frac14 101 in

L frac14 9 Dm frac14 909 in

r frac14 1727 Dm frac14 1744 in

a frac14 05ethDm 2rTHORN frac14 5eth101 3488THORN frac14 3306 in

SF

L

Dm

tr

a

βTL

Figure 2-54 Dimensions of head

Rc

Do

ro

tA

Figure 2-53 Dimensions of pipe bend

134 Pressure Vessel Design Manual

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 48: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

sin a frac14 a=ethL-rTHORN frac14 3306=eth909 - 1744THORN frac14 452

a frac14 2675

b frac14 90 a frac14 6325

bull Length of knuckles L1

L1 frac14 2rbethp=180THORN2eth1744THORNeth6325THORNethp=180THORN frac14 3850 in

bull Length of crown L2

L2 frac14 2Laethp=180THORN frac142eth909THORNeth2675THORNethp=180THORN frac14 8488 in

bull Diameter of blank necessary Db (Developed length)

Db frac14 L1 thorn L2 thorn 2 SFthorn 1 in

frac14 3850thorn 8488thorn 3thorn 1 frac14 12738

bull Per ASME Section VIII-1

FE frac14 75 t=Rf1 Rf=Ro

frac14 eth75THORNeth1THORN=eth1744THORN frac14 430

Since Ro frac14 N ie starting with flat plate the term(1 ndash Rf Ro) drops outSince FE 5 no heat treatment required

bull Per ASME Section VIII-2

εf frac14 100 LnDb=Di

frac14 100 Lneth127=100THORN frac14 239

Since FE gt 5 heat treatment is required

Example 2 Pipe BendPipe Size 4rdquo Sch 40

do frac14 45 in

tA frac14 0154 in

Rc frac14 6 in

bull Wall thinning after forming tBtB frac14 frac12Rc=ethRc thorn 5 doTHORNethtATHORN

frac14 frac126=eth6thorn 5eth45THORNeth154THORN frac14 0112 in

bull Forming strain εf (per ASME VIII-2)

εf frac14 maxr=Rf

tA-tB

tA 100

Where

DOd

(a)

(b)

(c)

(d)

(f)

t

Original Configuration

Flare

Swage

Upset (OD Match)

Upset (Neither ID nor OD Match)

tf

tf

L

Lf

Lf

df Df

df Df

tf

Lf

df Df

df Df

tf

Lf

(e)

Upset ( ID Match)

df Df

tf

Lf

Figure 2-55 Cold forming operations for flaring swap-ing and upsetting of tubing

General Design 135

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 49: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Rf frac14 Rc thorn ro 5 tB

frac14 6thorn 225 056 frac14 8194 in

εf frac14 max225=8194

0154 0112THORN=0154

$100 frac14 275

Notes

1 This procedure is for carbon steel and low alloymaterial only

2 As far as ASME Code is concerned there is nodifference between fiber elongation FE and form-ing strain εf In ASME VIII-1 it is called fiberelongation In ASME VIII-2 it is called formingstrain In reality the only way to determine actualfiber elongation is to remove a sample section ofmaterial macroetch the sample and view undera microscope

3 For formed vessel heads the fiber elongation in theknuckle will always govern However the FE shouldbe calculated for the crown radius as well

4 For pipe bends the inside of the pipe bend getsthicker while the outside of the bend tends to stretchthe material and thinning occurs The maximum FEis at the far outside of the bend also known as theextrados

5 Requirements for heat treatment

For P No 1 Groups 1 amp 2

a All material with a FE gt 5 should be heat treatedexcept following

b FE can be as high as 40 providing none of thefollowing conditions existbull Vessel is in lethal servicebull Impact testing is not requiredbull t gt 0625 inbull Forming temperature is between 250F to 900F

For all other material groups

6 For all other material see applicable materialsections of ASME Code

7 When heat treatment is required it shall be stressrelieved

8 Normalizing is only required when called out bycustomer or material specifications

9 If the section is hot formed above the normalizingtemperature and allowed to air cool no furtherheat treatment is required

10 Requirements per ASME Section VIII Division 1shall be per UCS-79

11 Requirements per ASME Section VIII Division 2shall be per Table 61

136 Pressure Vessel Design Manual

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 50: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

Table 2-25Formulas for calculating forming strains

Type of Part Being Formed Forming Strain

Heads and conical sections e formed by spinning or dishingεf frac14 100ln

Dh

Do 2t

Shell e cylinders formed from plateεf frac14 50t

Rf

1 Rf

Ro

Heads and conical sections e formed by pressingεf frac14 75t

Rf

1 Rf

Ro

Tubing and pipe-bendsεf frac14 max

roRf

tA tB

tA

100

Tubing and pipe-flares swages and upsets outside diameter hoop strain

εf frac14D Df

D

100

inside diameter hoop strain

εf frac14d df

d

100

axial strain

εf frac14L Lf

L

100

radial strain

εf frac14t tft

100

General Design 137

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual

Page 51: Pressure Vessel Design Manualpvmanage.com/wp-content/uploads/2018/12/General-Design... · 2018-12-08 · arbitrary value. The vessel fabricator is then responsible to verify that

References

[1] ASME Boiler and Pressure Vessel Code SectionVIII Division 1 2010 Edition American Societyof Mechanical Engineers

[2] Harvey JF Theory and Design of Modern PressureVessels 2nd Edition Van Nostrand Reinhold Co1974

[3] Bednar HH Pressure Vessel Design Handbook VanNostrand Reinhold Co 1981

[4] Brownell LE Young EH Process equipment designJohn Wiley and Sons Inc 1959 Section 62pp 157ndash159

[5] Watts GW Lang HA The Stresses in a PressureVessel with a Flat Head Closure ASME Paper No51-Andash146 1951

[6] Burgreen D Design methods for power plant struc-tures C P Press 1975

[7] Manual of Steel Construction 8th Edition AmericanInstitute of Steel Construction Inc 1980

[8] ASME Boiler and Pressure Vessel Code SectionVIII Division 2 2010 Edition American Societyof Mechanical Engineers

[9] Levinson IS Statics and Strength of Materials Pren-tice Hall Inc 1971 Chapter 16

[10] Troitsky MS Tubular Steel Structures Theory andDesign 2nd Edition James F Lincoln Arc WeldingFoundation 1990 Chapter 2

[11] Dambski JW Interaction Analysis of CylindricalVessels for External Pressure and Imposed Loads

ASME Technical Paper 80-C2PVP-2 AmericanSociety of Mechanical Engineers 1990

[12] Harvey JF Theory and Design of Pressure VesselsVan Nostrand Reinhold Co 1985 Chapter 8

[13] AWWA D-100-96 Welded Steel Tanks for WaterStorage American Water Works Association6666 W Quincy Ave Denver CO 80235 Section40

[14] Jawad MH Farr JR Structural analysis and Designof Process Equipment 2nd Edition John Wiley andSons 1989 Chapter 53

[15] Bednar HH Pressure Vessel Handbook 2ndEdition Van Nostrand Reinhold Co 1986 48ndash55

[16] Kerns GD New charts speed drum sizing Petro-leum Refiner July 1960

[17] Jawadekar SP Consider corrosion in LD calcula-tion Chemical Engineering December 15 1980

[18] Abakians K Nomographs give optimum vessel sizeHydrocarbon Processing and Petroleum RefinerJune 1963

[19] Gerunda A How to size liquid-vapor separatorsChemical Engineering May 4 1981

[20] Brownell LE Young EH Process EquipmentDesign John Wiley amp Sons Inc 1959Chapter 5

[21] Galambos Theodore V Guide to Stability DesignCriteria for Metal Structures John Wiley amp SonsINC 1998 Chapter 14

138 Pressure Vessel Design Manual