seive column design

8/13/2019 Seive Column Design

1/103

Sieve ColumnDesign


2/103

Given: Ethanol-Water System

D = 300,000 L/day

XF= 0.10 by volume

XB= 0.01 % by volume

XD= azeotropic concentration

95.6 % ETOH - 4.4 % H20 by wt.

Operating Conditions:

25 oC and 1 atm


3/103

Seive Column Design

TRAY

Tray Spacing, Tray thickness, Number ofholes, hole diameter, Pitch

COLUMN

Number of Equilibrium Stages andColumn Diameter

DOWNCOMER ASSEMBLY

Weir length, Weir height, DowncomerLength


4/103


5/103

Data TOP BOTTOM

Pressure, (psia)

Temperature, (o

C)L (lb/cu. ft)

V (lb/cu. ft)

Internal reflux

Max vapor, Qv(lb/hr)

Max liquid, QL (lb/hr)

Max vapor, Qv(cu. ft/hr)

Max liquid, QL(cu. ft/hr)Max liquid, QL(gpm)

Surface Tension, (dynes/cm)

Tray Spacing, (ft.)


6/103

XD= 0 8947

18.016kg

14.4kg

46.069kg

195.6kg

46.069kg

195.6kg

fraction)(molXDmolmol

mol


7/103

Convert XF= 0.01 by vol. to by percent by mole

From Perrys (Table 2-28)H2O@ 25

oC = 997.045 kg/m3

From (Table 2-30)

))/1(1(

2

14

3C

CTEtOH

C

C


8/103


9/103

Convert XF= 0.01 by vol. to by percent by mole

From Perrys (Table 2-28)H2O@ 25

oC = 997.045 kg/m3

From (Table 2-30)

))/1(1(

2

14

3C

CTEtOH

C

C

))92.513/15.2981(1(

2331.0

27627.0

648.1

EtOH

305082236.17

m

kmolEtOH


10/103

kg

kmol

m

kg

m

kmol

m

kmol

XF

016.18

1045.99790.00508.1710.0

0508.1710.0

33

3

0331.0FX


11/103

Convert XBinto mole fraction:

Since given is XB= 0.01% by volume- the fraction of ethanol in the bottoms

can be assumed to be negligible

Thus, assume the temperature in the

bottom plate can be assumed to be 100 oC- the boiling point of water at 1 atm


12/103

From Table 2-28 of Perrys (p.2-91)

3

3

3100

7492.59

28.3

1

1

2.2365.9580

2

f t

lb

f t

m

kg

lb

m

kgCatOH

37492.59

f tlb

LV


13/103

3

92.513

15.37311

100 4429.15

27627.0

648.12331.00

m

kmolCatetOH

kg

kmol

m

kg

m

kmol

m

kmol

XB

016.18

1365.9580001.014429.150001.0

4429.150001.0

33

3

5109035.2

xXB

Solving for XB


14/103

Determination of Densities

Saturation temperature at azeotropic concentrationTsat= 78.10

oC

Interpolating from Table 2-256 of Perrys

Tsat= 273.15 + 78.10 = 351.25 K


15/103


16/103

351.25 0.001 33505


17/103

Determination of Densities

Saturation temperature at azeotropic concentrationTsat= 78.10

oC

Interpolating from Table 2-256 of Perrys

Tsat= 273.15 + 78.10 = 351.25 K

kg

mxVf

3

31033505.1

3

3

3 6985.462.2

28.3

11

f t

lb

kg

lb

f t

m

kg

mVF

LV


18/103

Assuming that the gas phase behaves ideally,

manipulation of the ideal gas equation:

L

g

KKmol

atmL

atmmol

g

RT

MP

V

mVT 5881.0

15.3730821.0

1016.18

3

3 28.3

1

1

1000

1000

2.25881.0

f t

m

m

L

g

lb

L

gVT

30167.0

f t

lbVT


19/103

3

3 28.31

11000

12.2

100014951.1

15.2731.780821.0

11150.43

f tm

mL

k glb

gk g

Lg

KKmol

atmL

atm

mol

g

RTMP

Vm

VB

VB

30932.0

f tlb

VB


20/103

Data TOP BOTTOM

Pressure, psia

Temperature,o

CL lb/cu. ft

V lb/cu. ft

Internal reflux

Max vapor, lb/hr

Max liquid, lb/hr

Max vapor, cu. ft/hr

Max liquid, cu. ft/hrMax liquid, gpm

Surface Tension , dynes/cm

Tray Spacing, ft.


21/103

Data TOP BOTTOM

Pressure, psia 14.7 14.7

Temperature,o

CL lb/cu. ft

V lb/cu. ft

Internal reflux

Max vapor, lb/hr

Max liquid, lb/hr




Tray Spacing, ft.


22/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft

V lb/cu. ft

Internal reflux

Max vapor, lb/hr

Max liquid, lb/hr




Tray Spacing, ft.


23/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft

Internal reflux

Max vapor, lb/hr

Max liquid, lb/hr




Tray Spacing, ft.


24/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367

Internal reflux

Max vapor, lb/hr

Max liquid, lb/hr




Tray Spacing, ft.


25/103

MF= 0.0331(46.069) + (1 - 0.0381)(18.016)= 18.9446 g/mol

MD= 0.8947(46.069) + (1 - 0.8947)(18.016)= 43.1150 g/mol

MB= 2.9033x10-5

(46.069) + (1 - 2.9033x10-5

)= 18.0168 g/mol


26/103

OMB: F = D + B

hr

day

kg

kmol

m

kg

L

m

day

L

hrday

kgmol

mkg

Lm

dayLD

24

1

016.18

1974.972

1000

1000,3008947.01

241

069.461036.749

10001000,3008947.0

3

3

3

3

Material Balances

hrlbmolD 095.550


27/103

CMB: FXF= DXD+ BXB

5

109033.2095.550

8947.0095.5500331.0

xhr

lbmol

F

hr

lbmolF

hrlbmolB

hrlbmol

F

626.332,14

721.882,14


28/103

Determination of L and V (McCabe-ThieleGraphical Method)

D

Lo

RD

min)50.105.1( DDactual RR

ESOL Eqn:

ND

Dn X

R

RY

1

1

1

D

D

R

X

Dn XV

DX

V

L

SSOL Eqn:

1n

Y

B

B

mB

B

R

X

XR

R 1

Bm XV

BX

V

L


29/103

XF = 0.0331

77oF

q = 4

q - line

XD = 0.8947

F

Fvap

H

HH

q

33.1

3

4

1

q

qm


30/103

XF = 0.0331

XD = 0.8947

ESOL for RDmin

70769.01min

min DD

RRESOLofslope

RDmin = 2.4211

2666.01

intmin

D

D

R

XESOLofy RDmin = 2.3551

RDmin,ave = 2.3881RDactual =

1.50(RDmin)

RDactual = 3.58215


31/103

XF = 0.0331

XD = 0.8947

7993.01 Dactual

Dactualactual

RRESOLofslope

XB

N = 20

Feed Stage, NF= 17

2706.11

B

B

RRSSOLofslopeRB =3.6957


32/103

58215.3D

LoRD

L = 3.58215D = 3.58215(550.095)

L = 1970.523 lbmol/hr

Balance over Top Plate:

V = L + D

V = 1970.523 + 550.095

V = 2520.618 lbmol/hr

V

L

V


33/103

B

B

R

R 1

mm

mm

25.4

4.5Slope of SSOL, = 1.2706

RB= 3.6957 =B

V

332.626)3.6957(14,3.6957B V

V

VBL lbmol/hr67,301.712L

= 52,969.086 lbmol/hr

= 14,332.626 + 52,969.086

Balance Over Bottom Plate

V

L

V


34/103

N = 20

Feed Stage = 17


35/103

FLOW RATES FOR TOP PLATE

lb/hr84,959.11

1150.431970.523L

lbmol

lb

hr

lbmol

/sft0.50543600

1

6985.46

184,959.1 3

3

s

hr

lb

ft

hr

lb

gpm40.67min1

60

785412.3

1

283.3

10000.5054

3

3

s

L

gal

ft

L

s

ft

lb/hr5108,676.441150.43

2520.618V

lbmol

lb

hr

lbmol

/sft323.9053600

1

0932.0

15108,676.44

33

s

hr

lb

ft

hr

lb


36/103

FLOW RATES FOR BOTTOM PLATE

lb/hr4851,212,561.1

0168.1867,301.712L lbmol

lb

hr

lbmol

/sft5.6373600

1

7492.59

14851,212,561. 3

3

s

hr

lb

f t

hr

lb

gpm453.591min1

60

785412.3

1

283.3

10005.637

3

3

s

L

gal

ft

L

s

ft

lb/hr86954,333.42

0168.18

52,969.086V

lbmol

lb

hr

lbmol

/sft7223.2323600

1

0167.0

186954,333.42 3

3

s

hr

lb

ft

hr

lb


37/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367

Internal reflux 3.58215 3.6957

Max vapor, lb/hr

Max liquid, lb/hr




Tray Spacing, ft.


38/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 108,676.445 954,333.429

Max liquid, lb/hr




Tray Spacing, ft.


39/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 108,676.445 954,333.429

Max liquid, lb/hr 84,959.1 1,212,561.5




Tray Spacing, ft.


40/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 108,676.445 954,333.429

Max liquid, lb/hr 84,959.1 1,212,561.5

Max vapor, cu. ft/hr 323.905 7,225.232



Tray Spacing, ft.


41/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 108,676.445 954,333.429

Max liquid, lb/hr 84,959.1 1,212,561.5

Max vapor, cu. ft/hr 323.905 7,225.232

Max liquid, cu. ft/hr 0.5054 5.637Max liquid, gpm


Tray Spacing, ft.


42/103

Data TOP BOTTOM


Temperature,o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 108,676.445 954,333.429

Max liquid, lb/hr 84,959.1 1,212,561.5

Max vapor, cu. ft/hr 323.905 7,225.232

Max liquid, cu. ft/hr 0.5054 5.637Max liquid, gpm 40.67 453.5941


Tray Spacing, ft.


43/103

For Surface Tension:

mmNm /40.71

At 100oC: mmNwater /91.58

mmN

mmN

etOH

water

/55.17

/32.59

894701244.0D

X

At 78.1oC:

105298756.02 OHX


44/103

6277.3

1

log

log1

log

10

)0185.0)(32.59(2

0627.055.17

25.351

21.44

)0627.0)(8947.0()0185.0)(1053.0(

0627.08947.00185.01053.01010

3

2

32

1

2

w

w

x

w

w


45/103

cm

dyne

xx

x

water

water

etOH

w

ww

w

w

9313.17

)55.17(9848.0)32.59(0152.0

9848.00152.01

0152.0

103567.2103567.2

103567.21

25.025.0

44

4

4

1

2


46/103

Data TOP BOTTOM


Temperature,

o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 10345.44 90840.23

Max liquid, lb/hr 8087.69 115420.53

Max vapor, cu. ft/hr 30.83 687.56


Surface Tension , dynes/cm 17.93 58.91

Tray Spacing, ft.


47/103

Data TOP BOTTOM


Temperature,

o

C 78.1 100L lb/cu. ft 46.6985 59.7491

V lb/cu. ft 0.0932 0.0367


Max vapor, lb/hr 10345.44 90840.23

Max liquid, lb/hr 8087.69 115420.53

Max vapor, cu. ft/hr 30.83 687.56


Surface Tension , dynes/cm 17.93 58.91

Tray Spacing, ft. 1.5 1.5


48/103

TOWER DIAMETER

CALCULATIONS


49/103

*Assuming a non-foaming system* Based on 80% flooding and the use of splash baffle

5.0

L

V

FV

LP

0349.06985.46

0932.0

445.108676

91.84959 5.0

0315.7492.59

0367.0

4286.954333

485.1212561 5.0

TOP PLATE BOTTOM PLATE


50/103

From Figure 13.21 of Van Winkle,With a Tray Spacing of 1.5 ft


51/103

0.275

0.280


52/103

From Figure 13.12 of Van WinkleWith a Tray Spacing of 1.5ft

275.0CP

280.0CP 269.0

20

93.17275.0

,

8.0

,

corrC

corrC

P

P

348.020

91.58280.0

,

8.0

,

corrC

corrC

P

P


53/103

For 100% flood,

fpsU

U

VN

VN

015.6

0932.0

0932.06985.46269.0

5.0

fpsU

U

VN

VN

047.14

0367.00367.07492.59348.0

5.0

5.0

V

VLCVN PU


54/103

Computing for vapor flow net area ANfor 80 %of flood,

8.0VNV

NU

QA

ftsqAN 312.67

8.0015.6905.323

ftsqAN 231.643

8.0037.14

232.7223


55/103

Assume Ad= 0.1A,Thus A = AN+ 2Ad= AN+ 0.2A

A = 67.312 + 0.2AA = 84.14 sq. ft.

A = 643.231 + 0.2AA = 804.039 sq. ft.

From

5.0

2 44

ADDA

D = 10.35 ft D = 31 ft


56/103

Check the validity of the assumption from Table 14.2

Table 14.2 Recommended Limits: Tray and Column design

Perforated Trays

Column diameter

basis: % flood

Tray Spacing

Tray

Flow arrangementGeneral

med. diam. 6-12 ft

large diam. 12-24 ft

Tray layout

1-24ft

80-85% NF

70-75%

Fig. 13.21

12-36 in.Col. diam. 2.0-4.0ft; 12-18 in

Col. diam. 5.0-24 ft; 24-36 in

check: liquid backup, entrainment

(table 14.3)

Cross flow

DP

Multiple pass

Hole diam.: 1/81/2 in.Hole area: 6-15% col. Area

Spacing: pitch/hole diam., 2-4

tray thickness: 16 gage to in.

AssumedTray Spacingless thanminimum fora 10ftcolumn

Assumedwas 18in


57/103


Change tray spacing to 36 inches (3ft)

Read Pc from Table 13.2


58/103

0.48

0.49


59/103


Change tray spacing to 36 inches (3 ft)

Read Pc from Table 13.2

Pc= 0.48

Following previously done calculations

D = 23.5 ft

Pc= 0.49

D = 7.5 ft


60/103

Check for Percent Flood

AVN

V

AUQflood %

)51.10)(321.45)1.0(2321.45(

905.323%

flood

)525.24)(125.433)(1.0(2125.433(

232.7223%

flood

%85% flood %85% flood


61/103

A = 45.321 ft2 A = 433.125 ft2

A = 0.1(A)

= 4.5321 ft2

AA= A2(0.1)A= 2 36.257 ft2

A = 0.1(A)

= 4.5321 ft2

AA= A2(0.1)A= 346.5 ft2


62/103

D = 23.5 ft

D = 7.5 ft


63/103

SEIVE TRAY

DESIGNCALCULATIONS


64/103

dhtp

P


65/103

Tray Spacing, Stray


66/103

From Table 14.2, create a pre-assumedTray Layout


67/103

Table 14.2 Recommended Limits: Tray and Column design

Perforated Trays

Column diameter

basis: % flood

Tray Spacing

Tray

Flow arrangement

General

med. diam. 6-12 ft

large diam. 12-24 ft

Tray layout

1-24ft

80-85% NF

70-75%

Fig. 13.21

12-36 in.

Col. diam. 2.0-4.0ft; 12-18 in

Col. diam. 5.0-24 ft; 24-36 in

check: liquid backup, entrainment

(table 14.3)

Cross flow

DP

Multiple pass

Hole diam.: 1/81/2 in.

Hole area: 6-15% col. Area

Spacing: pitch/hole diam., 2-4

tray thickness: 16 gage to in.

Hole clearance:

hole-tower wall, 1.5 in.

hole-weir, 2.0in., min

hole-apron, 2.0 in., min

Ave. dyanamic seal hds:

vacuum, 0.50.6 in.

atmospheric, 0.51.5 in.

pressure, 1.5-3.0 in.


68/103

From Table 14.2, create a pre-assumed

Tray Layout

Top Plate Bottom Plate

Tray Spacing 3.0 ft 3.0 ft

PlateThickness, tp

0.25 in 0.25 in

Hole

Diameter, dh

0.50 in 0.50 in

P/dhPitch, P

4

2 in

4

2 in


69/103

WEIR ANDDOWNCOMERASSEMBLY


70/103

Weir (Outlet Weir)

Downcomer

Weir Height, hw

Weir length, lw


71/103

Weir Length, lw

From Table 14.8, select hw= 3.0 in

Ad= 0.1A, 1.0A

Ad

From Table 14.10


72/103


73/103


74/103

Check for ENTRAINMENT

From Tower Diameter calculations

PF= 0.0349 PF= 0.0315

From Figure 13-26 (Entrainment Correlation)


75/103

0.165

0.160


76/103

Check for ENTRAINMENT

From Tower Diameter calculations

PF= 0.0349 PF= 0.0315

From Figure 13-26 (Entrainment Correlation)

Entrainment , moles/moles of downflow = 0.160 = 0.0165


77/103


78/103

5.2

w

Lw

l

QfF

5.2

w

L

l

Q

0946.25435.2

61.21

5.2

6931.1267.7

03.2415.2


79/103

From Figure 13.7

With L/D = 0.7267


80/103

L/D = 0.7267

1.020

1.022


81/103

From Figure 13.7

Fw= 1.022 Fw= 1.020

67.0

48.0

w

L

wow l

Q

Fh

inh

h

ow

ow

35.012525.5

67.40)022.1(48.0

67.0

inh

h

ow

ow

82.012085.17

591.453)020.1(48.0

67.0


82/103

h(equivalent surface tension head loss, in.)

hLdh

04.0

inh

h

0307.0

)50.0)(6985.46(

)93.17(04.0

inh

h

0789.0

)55.0)(7492.59(

)91.58(04.0


83/103

ho(equivalent head loss through holes, in.)

2

186.0

o

h

L

vo

C

Uh

Uh= velocity of vapor through holes

h

vh

A

QU

Ah= total hole area

From Table 14.8, with

10Ah


84/103

,

1.0A

Ah

2

2

6257.3

257.361.0

ftA

ftA

h

h

2

2

65.34

5.3461.0

f tA

ftA

h

h

fpsUh 46.20865.34232.7223

h

p

dt 50.0

50.0

25.0

50.050.0

25.0

89.34fps3.6257

323.905

hU

From Figure 13 18


85/103

From Figure 13.18,

725.0oC

725.0oC

Solving for ho

2

186.0

o

h

L

vo

C

Uh

inh

h

o

o

64.5725.0

34.89

6985.46

0932.0186.0

2

inh

h

o

o

45.9725.0

46.208

7492.59

0367.0186.0

2

t


86/103

1.0AA

h

50.050.0

25.0

in

in

d

t

h

p

0.50

0.725

From Figure 13 18


87/103

From Figure 13.18,

725.0oC

725.0oC

Solving for ho

2

186.0

o

h

L

vo

C

Uh

inh

h

o

o

64.5725.0

34.89

6985.46

0932.0186.0

2

inh

h

o

o

45.9725.0

46.208

7492.59

0367.0186.0

2

(relative foam density)


88/103

(relative foam density)

)( vaFf 5.0

)( vVAVA UF

UVA=vapor v eloci ty based on act ive area, fps

A

Q

A

QU v

A

v

VA8.0

93.8257.36

905.323VAU

87.205.346

232.7223VAU

5.0

)( vVAVA UF

727.2

)0932.0)(93.8( 5.0

VA

VA

F

F

0.4

)0367.0)(87.20( 5.0

VA

VA

F

F

From Figure 13 16


89/103

From Figure 13.16


90/103

0.56

0.55

From Figure 13 16


91/103

From Figure 13.16

56.0

55.0

Solving for total pressure drop

hhhhH owwT )( 0

inH

H

T

T

5802.7

0307.064.5)35.00.3(56.0

inH

H

T

T

5917.11

789.045.9)82.00.3(55.0

WEEP POINT


92/103

WEEP POINTCalculated (h

o+ h) > Theoretical (ho+ h)

(ho+ h)calc

6707.5)0307.064.5(

5289.9)0789.045.9(

(hw+ h

ow)

35.3)35.00.3(

82.3)82.00.3(

From Figure 13.22,


93/103

0.53

0.55

WEEP POINT


94/103

WEEP POINTCalculated (h

o+ h) > Theoretical (ho+ h)

(ho+ h

)

calc

6707.5)0307.064.5(

5289.9)0789.045.9(

(hw+ h

ow)

35.3)35.00.3(

82.3)82.00.3(

From Figure 13.22

53.0h(h o theo

55.0h(h o theo

LIQUID BACKUP IN DOWNCOMER


95/103

LIQUID BACKUP IN DOWNCOMER

d

dowwTD hhhHH1

2

= liquid gradient, in.

hd= equivalent head loss in downcomer, in.

d= froth density in downcomer

2

10003.0

dm

L

d A

Q

h

Adm

= minimum area of liquid flow in downcomer assembly

AAP= (apron clearance)(l

w)

Assume Apron clearance of 1.5 in


96/103

2691.0

)525.5(

12

1)5.1(

f tA

ft

in

ftinA

AP

AP

2136.2

)085.17(

12

1)5.1(

ftA

ft

in

f tinA

AP

AP

2

10003.0

dm

L

d A

Q

h

inh

h

d

d

4.01.0

)691.0(100

67.4003.0

2

inh

h

d

d

135.0

)136.2(100

591.453

03.0

2


97/103

Assume: = 0.10 d= 0.5

Solving for HD

inH

H

D

D

99.10

5.0

10104.0

2

10.035.00.35802.7

inH

H

D

D

5967.15

5.0

1

135.02

10.0

82.00.35917.11

LIQUID RESIDENCE TIME IN DOWNCOMER


98/103

LIQUID RESIDENCE TIME IN DOWNCOMER,

rateflowdowncomerofvolume

ssft

in

ft

inft 2126.8/5054.0

12

1

)99.10(5321.43

2

ssft

in

ftinft

987.9/637.5

12

1)5967.15(3125.43

3

2

L

Dd

QHA

SUMMARY


99/103

TOP BOTTOM

Tower diameter 7.5 ft 23.5 ftTray spacing 3 ft 3 ft

Active area 36.257 ft2 346.5 ft2

Area of holes 3.6257 ft2 34.65 ft2

Area downcomer 4.5321 ft2 43.3125 ft2

Ah/A 0.08 0.08

Ad/A 0.1 0.1

Ah/AA 0.1 0.1

dh 0.5 in 0.5 in

lw 5.525 ft 17.085 fthw 3.0 in 3.0 in

Tray thickness 0.25 in 0.25 in

Downcomer clearance

SUMMARY

SUMMARY Z = 60 ft


100/103

SUMMARY

N = 20

DISTILLATION COLUMN

NF= 17

DT= 7.5 ft

DB= 23.5 ft

TOTAL CONDENSER ANDPARTIAL REBOILER

Z = 60 ft

SUMMARY


101/103

SUMMARY

TRAY LAYOUT

Stray = 3 ft

Top and Bottom Plates

dh = 0.50 in

tp = 0.25 in

P = 2 in

Number ofholes=

SUMMARY


102/103

SUMMARY

DOWNCOMER ASSEMBLY

Top Plate

hw= 3 in

lw = 5.525 ft

R f


103/103

References:

Barrientos, Melvin Buensalido.

Foust, Alan S., et al. Principles of Unit Operations. 2nded. Singapore:John wiley & Sons. 1980

McCabe, Warren L., et al. Unit Operations for Chemical Engineers. 7th

ed. USA: McGraw-Hill Inc. 2006.

Molina, Claudia Arabelle.

Perry, Robert H., and Don W. Green. Perrys Chemical EngineeringHandbook, 7thed. USA: McGraw-Hill, Inc. 1997.

Van Winkle, Matthew. Distillation.

seive column design

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