chapter13 - valvblending
TRANSCRIPT
Petroleum Refining – Chapter 13: Product Blending
1
Chapter 13
Product Blending
Introduction The major refinery products produced by blending are:
- Gasoline
- Jet fuels
- Diesel fuel
- Furnace oils.
- Residual fuels.
- Heating oils
- Lubricating oils
More restrictions on
product specs
Refinery sources of gasoline (blending components)
- Straight-run gasoline (CDU naphtha).
- Coker gasoline
- FCC/TCC gasoline
- Hydrocracker gasoline (hydrocrackate)
- Reforming (reformate)
- Alkylation (alkylate)
- Polymerization (polymerate)
- Isomerization (isomerate)
- ARDS/isomax gasoline
- H-oil gasoline
- Thermal cracker gasoline.
- Aromatic concentrate
- C4+ Gases
- Other
These have different molecular contents and performance
qualities (RON, MON, RVP, API, BP range, etc.) as shown in
Table 13.1.
They must be blended into various grades that meet market
demands.
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
2
TABLE 13.1: Blending Component Values for Gasoline Blending Streams.
No Component RVP (psi) MON RON °API
1. i-C4 71.0 92.0 93.0
2. n-C4 52.0 92.0 93.0
3. i-C5 19.4 90.8 93.2
4. n-C5 14.7 72.4 71.5
5. i-C6 6.4 78.4 79.2
6. LSR gasoline (C5-180°F) 11.1 61.6 66.4 78.6
7. LSR gasoline Isomerized, once-through 13.5 81.1 83.0 80.4
8. HSR gasoline 1.0 58.7 62.3 48.2
9. Lt hydrocrackate 12.9 82.4 82.8 79.0
10. Hydrocrackate, C5-C6 15.5 85.5 89.2 86.4
11. Hydrocrackate, C6-l90 °F 3.9 73.7 75.5 85.0
12. Hydrocrackate, 190-250 °F 1.7 75.6 79.0 55.5
13. Hvy hydrocrackate 1.1 67.3 67.6 49.0
14. Coker gasoline 3.6 60.2 67.2 57.2
15. Lt thermal gasoline. 9.9 73.2 80.3 74.0
16. C6+ lt thermal gasoline. 1.1 68.1 76.8 55.1
17. FCC gasoline, 200-300 °F 1.4 77.1 92.1 49.5
18. FCC C5+ gasoline 4.4 76.8 92.3 57.2
19. Hydrog lt FCC gasoline, C5+ 13.9 80.9 83.2 51.5
20. Hydrog C5-200 °F FCC gasoline 14.1 81.7 91.2 58.1
21. Hydrog 1t FCC gasoline, C6+ 5.0 74.0 86.3 49.3
22. Hydrog C5+ FCC gasoline 13.1 80.7 91.0 54.8
23. Hydrog 300-400 °F FCC gasoline 0.5 81.3 90.2 48.5
24. Reformate, 94 RON 2.8 84.4 94.0 45.8
25. Reformate, 98 RON 2.2 86.5 98.0 43.1
26. Reformate, 100 RON 3.2 88.2 100.0 41.2
27. Aromatic concentrate 1.1 94.0 107.0
28. Alkylate, C3= 5.7 87.3 90.8
29. Alkylate, C4= 4.6 95.9 97.3 70.3
30. Alkylate, C3=, C4= 5.0 93.0 94.5
31. Alkylate, C5= 1.0 88.8 89.7
32. Polymer 8.7 84.0 96.9 59.5
33. C5+ TCC gasoline 4.0 76.6 85.5
34. C6+ TCC gasoline 2.6 75.8 84.3
These values are provided for illustration and cannot be generalized.
Petroleum Refining – Chapter 13: Product Blending
3
Blending components must meet all desired
specifications like boiling point, specific gravity, RVP,
research octane number (RON) and motor octane number
(MON) to provide feedback control of additives and
blending streams.
Basic intermediate streams can be blended to produce a
variety of on-spec finished products.
For example, naphtha can be blended into either gasoline
or jet fuel, depending upon the product demand.
The objective of product blending is to allocate the
available blending components in such a way as to meet
product demands and specifications at the least cost and
to produce incremental products which maximize overall
profit.
For example, if a refiner sells about one billion gallons of
gasoline per year (about 65,000 BPCD), a saving of one-
hundredth (1/100) of a cent per gallon results in an
additional profit of $100,000 per year.
Blending for API gravity
API Gravities are not linear and therefore can not be
averaged.
Specific gravity can be volume Averaged.
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
4
Example 13.1: Blending for API
Calculate the API of a blend from
1,000 bbls oil 30 ºAPI
3,000 bbls oil 40 ºAPI
Solution:
141.5 141.5= = 0.8251 sp.gr.
API + 131.5 30 + 131.5
141.5 141.5= = 0.8762 sp.gr.
API + 131.5 40 + 131.5
Ave. sp. gr. = 0.25(0.8251) + 0.75(0.8762) = 0.8634
API = (141.5/ 0.8634)-131.5 = 32.38 √
If you average the API then the answer is
0.25 x 30 + 0.75 x 40 = 37.5 (which is wrong)
Blending for Initial & Final BP
The initial boiling point of the blend equals the lowest of
the blending stocks and the final boiling point equals the
highest.
Petroleum Refining – Chapter 13: Product Blending
5
Example 13.2: Blending for Boiling Point
Calculate the initial and final boiling points of the blend from
the following blending stocks,
LSR gasoline (C5 – 180 ºF)
HSR gasoline (200 – 380 ºF)
FCC gasoline (200 – 300 ºF)
Blend (C5 – 380 ºF)
Blending for Reid Vapor Pressure (RVP)
The theoretical method for blending to the desired RVP
requires the average molecular weight of each of the
streams to be known.
A more convenient way developed by Chevron Research
Company is to use ‘Vapor Pressure Blending Indices’
(VPBI) compiled as a function of the RVP of the
blending streams as shown in Table 13.2.
The RVP of the blend is closely approximated by the
sum of all the products of the volume fraction (Xv) times
the VPBI for each component.
(VPBI)blend = ∑ Xvi (VPBI)i
The desired RVP of a gasoline is obtained by blending n-
butane with (C5 – 380°F) naphtha.
If the volume of the n-butane to be blended for a given
RVP is desired, then
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
6
Table 13.2: Reid Vapor Pressure Blending Index Numbers for Gasoline and Turbine Fuels.
Vapor
Pressure,
psi
0.0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
0
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
0.00
1.00
2.37
3.94
5.65
7.47
9.39
11.4
13.4
15.6
17.8
20.0
22.3
24.7
27.1
29.5
32.0
34.5
37.1
39.7
42.3
45.0
47.6
50.4
53.1
55.9
58.7
61.5
64.4
67.3
0.05
1.12
2.52
4.11
5.83
7.66
9.58
11.6
13.7
15.8
18.0
20.3
22.6
24.9
27.3
29.8
32.2
34.8
37.3
39.9
42.6
45.2
47.9
50.6
53.4
56.2
59.0
61.8
64.7
67.6
0.13
1.25
2.67
4.28
6.01
7.85
9.78
11.8
13.9
16.0
18.2
20.5
22.8
25.2
27.6
30.0
32.5
35.0
37.6
40.2
42.8
45.5
48.2
50.9
53.7
56.5
59.3
62.1I
65.0
67.9
0.22
1.38
2.83
44.4
6.19
8.04
9.98
12.0
14.1
16.2
18.4
20.7
23.0
25.4
27.8
30.2
32.8
35.3
37.8
40.4
43.1
45.8
48.4
51.2
54.0
56.7
59.6
62.4
65.3
68.2
0.31
1.52
2.98
4.61
6.37
8.23
10.2
12.2
14.3
16.4
18.7
20.9
23.3
25.6
28.0
30.5
33.0
35.5
38.1
40.7
43.4
46.0
48.7
51.5
54.2
57.0
59.8
62.7
65.6
68.4
0.42
1.66
3.14
4.78
6.55
8.42
10.4
12.4
14.5
16.7
18.9
21.2
23.5
25.9
28.3
30.8
33.2
35.8
38.4
41.0
43.6
46.3
49.0
51.7
54.5
57.3
60.1
63.0
65.8
68.8
0.52
1.79
3.30
4.95
6.73
8.61
10.6
12.6
14.7
16.9
19.1
21.4
23.7
26.1
28.5
31.0
33.5
36.0
38.6
41.2
43.9
46.6
49.3
52.0
54.8
57.5
60.4
63.3
66.1
69.0
0.64
1.94
3.46
5.13
6.92
8.80
10.8
12.8
14.9
17.1
19.4
21.6
24.0
26.4
28.8
31.2
33.8
36.3
38.9
41.5
44.2
46.8
49.5
52.3
55.1
57.9
60.7
63.5
66.4
69.3
0.75
2.08
3.62
5.30
7.10
9.00
11.0
13.0
15.2
17.3
19.6
21.9
24.2
26.6
29.0
31.5
34.0
36.6
39.1
41.8
44.4
47.1
49.8
52.6
55.3
58.1
61.0
63.8
66.7
69.6
0.87
2.23
3.78
5.48
7.29
9.19
11.2
13.2
15.4
17.6
19.8
22.1
24.4
26.8
29.3
31.8
34.3
36.8
39.4
42.0
44.7
47.4
50.1
52.8
55.6
58.4
61.3
64.1
67.0
69.9
30
40
70.2
101
Example:
Calculate the vapor-pressure of a gasoline blend as follows
(nC4) 51.6
(iC4) 72.2
(C3) 190.0
138
210
705
Component
Volume
Fraction
Vapor
Pressure
psi
Vapor
Pressure
Blending
Index No.
Volume
Fraction
x
VPBI
Equation:
VPBI = VP1.25
n-Butane
Light Straight Run
Heavy Refined
Total
0.050
0.450
0.500
1.000
51.6
6.75
1.00
7.40
138
10.9
1.00
12.3
6.90
4.90
0.50
12.3
From the brochure, “31.O°API Iranian Heavy Crude Oil,” by arrangement with Chevron
Research Company. Copyright © 1971 by Chevron Oil Trading Company.
Petroleum Refining – Chapter 13: Product Blending
7
V1 (VPBI)1 + V2 (VPBI)2 + …...……+ V0 (VPBI)0
= (V1 + V2 + … + V0) (VPBI)m
where
V0 = Volume (bbl) of n-butane.
V1 = Volume (bbl) of blending stock 1.
1, 2, 3 = blending stocks 1, 2, 3, etc.
(VPBI)m = VPBI of the mixture
RVPm1.25 = [V1(RVP1)1.25 + V2(RVP2)1.25 + ….]/ total volume
Blending for Octane Number
Octane numbers are blended on a volumetric basis.
True octane numbers do not blend linearly. Therefore,
blending octane numbers are used.
Those are numbers which, when added on a volumetric
average basis, will give the true octane of the blend.
Blending octane numbers are based upon experience.
True octane is defined as the octane number obtained
using a CFR test engine.
The formula used for calculations is:
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
8
Vt (ON)t = ∑ Vi (ON)i
where,
Vt = Total gasoline blended (bbl).
Vi = Volume of component i (bbl).
(ON)t = Desired octane of blend.
(ON)i = Blending octane number of component i.
If n-butane alone is not sufficient to increase the Pool
octane number of the gasoline, different ways are used to
improve the octane number of the gasoline. These are:
1. Increase severity of reforming to produce a 98.8 or
100 RON (clear) reformate.
Note: This is not attractive because the aromatics
content of the gasoline would increase and the
volume would decrease.
2. Use an octane blending agent, such as MTBE or
ETBE (Table 13.3) to improve the pool octane.
Table 13.3: Blending values of octane improvers Compound Formula MW API Tb (ºF) RVP (psi) Flash
point (ºF)
RON MON
Methanol
Ethanol
TBA
MTBE
ETBE
TAME
TEL
CH4O
C2H6O
C4H10O
C5H12O
C6H14O
C6H14O
C8H20Pb
32
46.1
74.1
88.1
102.2
102.2
323.4
46.2
46.1
47.4
58.0
56.7
53.7
3.143
148.5
173
180.4
131.4
159.8
185
239
40
11
6
9
4
1.5
0
53.6
53.6
39.2
-18.4
-2.2
12.2
199.4
135
132
106
118
118
111
10,000
105
106
89
101
102
98
13,000
Petroleum Refining – Chapter 13: Product Blending
9
Example 13.3 for RVP and Octane Number:
From the following stocks
1,250 bbls HSR gasoline
,750 bbls LSR gasoline
,620 bbls C5+ FCC gasoline
a. Calculate the amount of n-butane required to produce a
gasoline with and RVP of 9 psi.
b. Calculate the RON and MON for the blend?
c. Calculate the posted octane number (PON) if 10 V%
MTBE is added (keeping RVP at 9 psi).
Solution
RVP values are obtained from Table 13.1
VPBI values are obtained from Table 13.2
COMPONENT # BPD RVP
Table 13.1
VPBI
Table 13.2
BPD x VPBI
n-butane 2 W 52 139.64 139.64W
HSR gasoline 8 1250 1.0 1.0 1250.00
LSR gasoline 6 750 11.1 20.3 15225.00
C5+ FCC gasoline 18 620 4.4 6.37 3949.40
Total for blend 2620 + W 139.64W + 20424.4
∑ (BPD) ∑ (BPD.VPBI)
At 9.0 RVP, from Table 13.2, (VPBI)m = 15.6
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
10
(VPBI)m x ( )BPD BPDxVPBI
15.6 (2620 + W) = 20424.4 + 139.64 W
40872 + 15.6 W = 20424.4 + 139.64W
124.04 W = 20447.6
W = 04.124
6.23454
W = 165 BPD of n-butane
b.
Component # BPD Vol.
Frac. MON
Table 13.1
RON
Table 13.1
MON x
Vol. frac.
RON x
Vol. frac.
n-butane 2 165 0.0592 92.0 93.0 4.85 5.51
HSR gasoline 8 1250 0.4488 58.7 62.3 26.34 27.96
LSR gasoline 6 750 0.2693 61.6 66.4 16.59 17.88
C5+ FCC
gasoline
18 620 0.2226 76.8 92.3 17.10 20.55
Total for blend 2785 64.9 71.9
MON of the blend = ∑MON x vol. frac. = 64.9
RON of the blend = ∑RON x vol. frac. = 71.9
10 % is equal to 0.1(2785) = 278.5
Octane number values are obtained form Table 13.3
Component BPD Vol.
Frac.
MON RON MON x Vol.
frac.
RON x
Vol. frac.
n-butane 165 0.054 92.0 93.0 4.97 5.022
HSR gasoline 1250 0.408 58.7 62.3 23.95 25.42
LSR gasoline 750 0.245 61.6 66.4 15.1 16.27
C5 FCC gasoline 620 0.202 76.8 92.3 15.51 18.64
MTBE 278.5 .091 101 118 9.19 10.74
Total 3063.5 68.72 76.1
PON of the blend = (vol. frac. x RON) (vol.frac. x MON)
2
=
76.1 68.72
2
= 72.4
Petroleum Refining – Chapter 13: Product Blending
11
BLENDING FOR OTHER PROPERTIES
Several methods exist for estimating the physical
properties of a blend from those of the blending stocks.
One of the most convenient methods of estimating
properties, that do not blend linearly, is to substitute for
the value of the inspection to be blended another value
which has the property of blending approximately linear.
Such values are called blending factor or index.
The Chevron Research Company has compiled factors or
index numbers for,
Viscosities, Table 13.4
Flash points, Table 13.5
Aniline points, Table 13.6
Pour point, Table 13.7
Blending for Viscosity
Viscosity blending is more complicated than the others.
It is not an additive property and it is necessary to use
special techniques to estimate the viscosity of a blend
from the viscosities of its blending stocks.
The method most commonly accepted is the use of
special charts developed by and obtainable from ASTM.
The viscosity factor of the blend can be calculated using
the equation:
(VF) blend = ∑ Xvi (VF)i
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
12
where,
Xvi = Volume fraction.
(VF)i = Viscosity factor for component i (Table 13.4).
(VF)blend = Viscosity factor for the blend.
Blending of kinematic viscosities (centistokes, cSt) may
be done at any temperature, but the viscosities of all
components of the blend must be at the same
temperature.
Blending of Saybolt universal viscosities also may be
done at any temperature and interchangeably with
kinematic viscosities at the same temperature.
Table 13.4 may be used to convert viscosities expressed
in centistokes (cSt) to Saybolt Universal Seconds (SUS)
and vice versa.
Viscosity factors also are given in Table 13.4 for
viscosities expressed in Saybolt Furol Seconds (SFS).
Saybolt Furol viscosities are blended only at 122°F.
If SFS viscosities are at any other temperature, they must
be converted to centistokes or SUS before blending.
Viscosity factors for SFS at 122 °F may be used
interchangeably with viscosity factors for SUS at 130 °F
and with centistokes at 130 °F.
Table 13.4 may be used also to convert viscosities in SFS
at 122 °F to either kinematic or Saybolt Universal
viscosities at 130 °F.
Other viscosity units include
- Redwood sec
Petroleum Refining – Chapter 13: Product Blending
13
- Redwood Admiralty Seconds
- Redwood No.1 Seconds
The viscosity of a blend can also be estimated by API
Procedure 11A4.3 in the API Technical Data Book -
Petroleum Refining.
Table 13.4 maybe digitized and the following equations
are obtained,
X1 = log (visc.1)
11 2
1 1
0.17011008+0.5237753 X
1+0.51237772 X 0.012329287 XVF
1 1 2 2
1 2
V VF V VF ...
V V ...blendVF
blend
2
blend blend
0.31495388+1.796746 (VF )log( . )
1 1.2634231 (VF ) 0.44952981 (VF )blendvisc
Example: using equations above
visc.i VFi Vi vol frac x factor
500 0.691 0.3333 0.230
300 0.669 0.3333 0.223
200 0.651 0.3334 0.217
Total 0.670
Log (viscblend) = 2.503
Visc = 318 cSt
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
14
Blending for Flash Point
The flash point index of a blend is given by
(FPBI) blend = ∑ Xvi (FPBI)i
where
(FPBI) blend = Aniline point blending index of the blend.
(FPBI)i = Aniline point blending index of component
i from Table 13.5.
Xvi = The volume fraction.
Blending for Aniline Point
The aniline point index of a blend is given by
(APBI) blend = ∑ Xvi (APBI)i
where
(APBI) blend = Aniline point blending index of the blend.
(APBI)i = Aniline point blending index of component
i from Table 13.6.
Xvi = The volume fraction.
Blending for Pour Point
Petroleum Refining – Chapter 13: Product Blending
15
The pour point index of a blend is given by
(PP) blend = ∑ Xvi (PPBI)i
where
(PP) blend = Pour point blending index of the blend.
(PPBI)i = Pour point blending index of component i
from Table 13.7.
Xvi = The volume fraction.
Example 13.4:
Calculate the viscosity, flash point, aniline point, and pour point of the blend from the
following blending stocks.
Stock bbls ASTM 50%
temp (ºF)
Viscosity Flash
point (ºF)
Aniline
point (ºF)
Pour
point (ºF)
A
B
C
5,000
3,000
2,000
575
425
500
430 SFS at 120 ºF
82.5 SUS at 130 ºF
2.15 cSt at 130 ºF
100
90
130
70
160
40 (mixed)
10
50
65
Solution:
a. Viscosity
Stock vol. frac. of
blend
Viscosity Factor
(T13.4)
vol. frac. x
Factor
A
B
C
0.5
0.3
0.2
430 SFS at 120 ºF
82.5 SUS at 130 ºF
2.15 cSt at 130 ºF
0.700
0.500
0.300
0.350
0.150
0.060
Total 1 0.560
Table 13.4 gives the following viscosities for a blend with a factor of 0.56
39.5 cSt at 130 ºF
183 SUS at 130 ºF
25.7 SFS at 122 ºF
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
16
b. Flash point
Stock vol. frac. of
blend
Flash point (ºF) Blending Index
(T13.5)
vol. frac. x
index
A
B
C
0.5
0.3
0.2
100
90
130
753
1,170
224
376.5
351
44.8
Total 1 772
Table 13.5 gives a flash point for the blend of 99.5 ºF for a blending index of 772.
c. Aniline Point
Stock vol. frac. of
blend
Aniline point (ºF) Blending Index
(T13.6)
vol. frac. x
index
A
B
C
0.5
0.3
0.2
70
160
40 (mixed)
347
855
-425
173.5
256.5
-85
Total 1 345
Table 13.6 gives for a blending index of 345 an aniline point for the blend of 69.5 ºF or a
mixed aniline point of 115 ºF.
d. Pour Point
Stock vol. frac. of
blend
ASTM 50%
temp (ºF)
Pour Point
(ºF)
Blending Index
(T13.7)
vol. frac. x
index
A
B
C
0.5
0.3
0.2
575
425
500
10
50
65
8
61
98
4
18.3
19.6
Total 1 41.9
The pour point of the blend is 41.9 ºF or 42 ºF.
Petroleum Refining – Chapter 13: Product Blending
17
TABLE 13.4: Viscosity Blending Index Numbers Factors for Volume Blending of Viscosities at Constant Temperatures
Corresponding to values of Kinematic Viscosity, Centistokes (cSt).
cSt
0.00
0.01
0.02
0.03
0.04
0.05
0.06
0.07
0.08
0.09
0.5
0.6
0.7
0.8
0.9
0.000
0.056
0.097
0.128
0.154
0.006
0.061
0.100
0.131
0.156
0.013
0.065
0.104
0.134
0.159
0.019
0.069
0.107
0.137
0.161
0.025
0.074
0.110
0.139
0.163
0.030
0.078
0.114
0.142
0.165
0.036
0.082
0.117
0.144
0.167
0.041
0.086
0.120
0.147
0.169
0.046
0.089
0.123
0.149
0.172
0.051
0.093
0.126
0.152
0.174
cSt
0.0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
1
2
3
4
5
6
7
8
9
0.176
0.290
0.342
0.375
0.398
0.416
0.431
0.443
0.453
0.194
0.297
0.346
0.378
0.400
0.418
0.432
0.444
0.454
0.210
0.303
0.350
0.380
0.402
0.419
0.433
0.445
0.455
0.224
0.309
0.353
0.383
0.404
0.421
0.434
0.446
0.456
0.236
0.314
0.357
0.385
0.406
0.422
0.436
0.447
0.456
0.247
0.320
0.360
0.387
0.408
0.423
0.437
0.448
0.457
0.257
0.325
0.363
0.390
0.410
0.425
0.438
0.449
0.458
0.266
0.329
0.366
0.392
0.411
0.426
0.439
0.450
0.459
0.275
0.334
0.369
0.394
0.413
0.428
0.440
0.451
0.460
0.283
0.338
0.372
0.396
0.414
0.429
0.442
0.452
0.461
cSt
0
1
2
3
4
5
6
7
8
9
10
20
30
40
50
60
70
80
90
0.462
0.515
0.543
0.561
0.575
0.585
0.594
0.601
0.608
0.470
0.519
0.545
0.563
0.576
0.586
0.595
0.602
0.608
0.477
0.522
0.547
0.564
0.577
0.587
0.596
0.603
0.609
0.483
0.525
0.549
0.566
0.578
0.588
0.596
0.603
0.610
0.489
0.528
0.551
0.567
0.579
0.589
0.597
0.604
0.610
0.494
0.531
0.553
0.568
0.580
0.590
0.598
0.605
0.611
0.499
0.533
0.555
0.570
0.581
0.591
0.599
0.605
0.611
0.503
0.536
0.557
0.571
0.582
0.592
0.599
0.606
0.612
0.508
0.538
0.558
0.572
0.583
0.592
0.600
0.607
0.612
0.511
0.541
0.559
0.573
0.584
0.593
0.601
0.607
0.613
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
18
cSt
0
10
20
30
40
50
60
70
80
90
100
200
300
400
500
600
700
800
900
0.613
0.648
0.667
0.680
0.689
0.697
0.703
0.708
0.713
0.618
0.651
0.669
0.681
0.690
0.698
0.704
0.709
0.714
0.623
0.653
0.670
0.682
0.691
0.698
0.704
0.709
0.714
0.627
0.655
0.671
0.683
0.692
0.699
0.705
0.710
0.715
0.631
0.657
0.673
0.684
0.692
0.700
0.705
0.710
0.715
0.634
0.659
0.674
0.685
0.693
0.700
0.706
0.711
0.715
0.637
0.661
0.675
0.686
0.694
0.701
0.706
0.711
0.716
0.640
0.662
0.676
0.687
0.695
0.701
0.707
0.712
0.716
0.643
0.664
0.678
0.688
0.696
0.702
0.707
0.712
0.716
0.646
0.666
0.679
0.688
0.696
0.702
0.708
0.713
0.717
cSt
0
100
200
300
400
500
600
700
800
900
1,000
2,000
3,000
4,000
5,000
6,000
7,000
8,000
9,000
0.717
0.743
0.757
0.767
0.775
0.780
0.785
0.790
0.793
0.721
0.745
0.758
0.768
0.775
0.781
0.786
0.790
0.794
0.724
0.747
0.759
0.769
0.776
0.781
0.786
0.790
0.794
0.727
0.748
0.761
0.770
0.777
0.782
0.787
0.791
0.794
0.730
0.750
0.762
0.770
0.778
0.782
0.787
0.791
0.795
0.733
0.751
0.763
0.771
0.778
0.783
0.787
0.791
0.795
0.735
0.752
0.764
0.772
0.778
0.783
0.788
0.792
0.795
0.737
0.754
0.765
0.772
0.779
0.784
0.788
0.792
0.796
0.739
0.755
0.765
0.773
0.779
0.784
0.789
0.792
0.796
0.741
0.756
0.766
0.774
0.780
0.785
0.790
0.793
0.796
cSt
0
1000
2000
3000
4000
5000
6000
7000
8000
9000
10,000
20,000
30,000
40,000
50,000
60,000
70,000
80,000
90,000
0.796
0.817
0.828
0.836
0.842
0.847
0.851
0.854
0.858
0.799
0.818
0.829
0.837
0.843
0.848
0.802
0.820
0.830
0.838
0.843
0.848
0.804
0.821
0.831
0.838
0.844
0.848
0.806
0.822
0.832
0.839
0.844
0.849
0.808
0.823
0.833
0.839
0.845
0.849
0.810
0.824
0.833
0.840
0.845
0.850
0.812
0.825
0.834
0.841
0.846
0.850
0.814
0.826
0.835
0.841
0.846
0.850
0.815
0.827
0.836
0.842
0.847
0.851
Petroleum Refining – Chapter 13: Product Blending
19
cSt
cSt cSt
100,000
200,000
300,000
400,000
500,000
600,000
700,000
800,000
900,000
0.860
0.877
0.887
0.894
0.899
0.903
0.906
0.909
0.912
1,000,000
2,000,000
3,000,000
4,000,000
5,000,000
6,000,000
7,000,000
8,000,000
9,000,000
0.914
0.928
0.937
0.942
0.947
0.950
0.953
0.956
0.958
10,000,000
20,000,000
30,000,000
40,000,000
50,000,000
60,000,000
70,000,000
80,000,000
90,000,000
0.960
0.973
0.980
0.985
0.989
0.992
0.995
0.997
0.999
Factors for Volume Blending of Viscosities at Constant Temperatures
Corresponding to values of Saybolt Universal Seconds (SUS).
SUS
0.0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
32
33
34
35
36
37
38
39
0.275
0.296
0.314
0.328
0.342
0.353
0.363
0.373
0.278
0.298
0.315
0.330
0.343
0.354
0.364
0.373
0.280
0.300
0.317
0.331
0.344
0.355
0.365
0.374
0.282
0.302
0.318
0.333
0.345
0.356
0.366
0.375
0.284
0.303
0.320
0.334
0.346
0.357
0.367
0.376
0.286
0.305
0.321
0.335
0.347
0.358
0.368
0.377
0.288
0.307
0.323
0.337
0.349
0.359
0.369
0.378
0.290
0.309
0.324
0.338
0.350
0.360
0.370
0.378
0.292
0.310
0.326
0.339
0.351
0.362
0.371
0.379
0.294
0.312
0.327
0.340
0.352
0.363
0.372
0.380
SUS
0
1
2
3
4
5
6
7
8
9
40
50
60
70
80
90
0.381
0.435
0.464
0.483
0.497
0.508
0.388
0.439
0.466
0.485
0.498
0.509
0.395
0.442
0.469
0.486
0.499
0.510
0.402
0.445
0.471
0.488
0.501
0.511
0.408
0.449
0.473
0.489
0.502
0.512
0.413
0.451
0.475
0.491
0.503
0.513
0.418
0.454
0.476
0.492
0.504
0.513
0.423
0.457
0.478
0.493
0.505
0.514
0.428
0.459
0.480
0.495
0.506
0.515
0.431
0.462
0.482
0.496
0.507
0.516
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
20
SUS
0
10
20
30
40
50
60
70
80
90
100
200
300
400
500
600
700
800
900
0.517
0.565
0.589
0.605
0.617
0.627
0.635
0.641
0.647
0.524
0.568
0.591
0.607
0.618
0.628
0.635
0.642
0.647
0.531
0.571
0.593
0.608
0.619
0.628
0.636
0.642
0.648
0.537
0.574
0.595
0.609
0.620
0.629
0.637
0.643
0.648
0.542
0.576
0.596
0.611
0.621
0.630
0.637
0.643
0.649
0.547
0.579
0.598
0.612
0.622
0.631
0.638
0.644
0.649
0.551
0.581
0.600
0.613
0.623
0.632
0.639
0.645
0.650
0.555
0.583
0.601
0.614
0.624
0.632
0.639
0.645
0.650
0.559
0.585
0.603
0.615
0.625
0.633
0.640
0.646
0.651
0.562
0.587
0.604
0.616
0.626
0.634
0.640
0.646
0.651
SUS
0
100
200
300
400
500
600
700
800
900
1,000
2,000
3,000
4,000
5,000
6,000
7,000
8,000
9,000
0.652
0.683
0.700
0.711
0.720
0.727
0.733
0.738
0.742
0.656
0.685
0.701
0.712
0.721
0.728
0.733
0.738
0.742
0.660
0.687
0.703
0.713
0.722
0.728
0.734
0.739
0.743
0.664
0.689
0.704
0.714
0.722
0.729
0.734
0.739
0.743
0.667
0.691
0.705
0.715
0.723
0.729
0.735
0.740
0.744
0.670
0.692
0.706
0.716
0.724
0.730
0.735
0.740
0.744
0.673
0.694
0.707
0.717
0.725
0.731
0.736
0.740
0.744
0.676
0.696
0.708
0.718
0.725
0.731
0.736
0.741
0.745
0.678
0.697
0.709
0.719
0.726
0.732
0.737
0.741
0.745
0.681
0.699
0.710
0.719
0.726
0.732
0.737
0.742
0.745
SUS
0
1000
2000
3000
4000
5000
6000
7000
8000
9000
10,000
20,000
30,000
40,000
50,000
60,000
0.746
0.770
0.783
0.792
0.799
0.804
0.749
0.771
0.784
0.793
0.799
0.805
0.752
0.773
0.785
0.793
0.800
0.805
0.755
0.774
0.786
0.794
0.800
0.806
0.758
0.776
0.787
0.795
0.801
0.806
0.760
0.777
0.788
0.795
0.802
0.807
0.762
0.778
0.789
0.796
0.802
0.807
0.764
0.779
0.790
0.797
0.803
0.807
0.766
0.781
0.790
0.797
0.803
0.808
0.768
0.782
0.791
0.798
0.804
0.808
Petroleum Refining – Chapter 13: Product Blending
21
SUS
SUS
SUS
SUS
70,000
80,000
90,000
0.809
0.813
0.816
100,000
200,000
300,000
400,000
500,000
600,000
700,000
800,000
900,000
0.819
0.838
0.849
0.856
0.862
0.867
0.870
0.874
0.877
1,000,000
2,000,000
3,000,000
4,000,000
5,000,000
6,000,000
7,000,000
8,000,000
9,000,000
0.879
0.895
0.904
0.911
0.915
0.919
0.923
0.925
0.928
10,000,000
20,000,000
30,000,000
40,000,000
50,000,000
60,000,000
70,000,000
80,000,000
90,000,000
0.930
0.944
0.952
0.957
0.961
0.965
0.968
0.970
0.972
Factors for Volume Blending of Viscosities at 130 °F Corresponding to values
of Saybolt Furol Seconds (SFS) at 122 °F.
SFS
at
122
°F
0
1
2
3
4
5
6
7
8
9
20
30
40
50
60
70
80
90
0.570
0.588
0.601
0.611
0.619
0.626
0.632
0.572
0.590
0.602
0.612
0.620
0.627
0.633
0.574
0.591
0.604
0.613
0.621
0.627
0.633
0.576
0.593
0.605
0.614
0.622
0.628
0.634
0.578
0.594
0.606
0.615
0.622
0.629
0.634
0.558
0.580
0.595
0.607
0.616
0.623
0.629
0.635
0.561
0.582
0.597
0.608
0.616
0.624
0.630
0.635
0.563
0.584
0.598
0.609
0.617
0.624
0.630
0.636
0.566
0.585
0.599
0.610
0.618
0.625
0.631
0.636
0.568
0.587
0.600
0.610
0.619
0.626
0.632
0.637
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
22
SFS
at
122
°F
0
10
20
30
40
50
60
70
80
90
100
200
300
400
500
600
700
800
900
0.637
0.669
0.686
0.697
0.706
0.713
0.719
0.724
0.728
0.642
0.671
0.687
0.698
0.707
0.713
0.719
0.724
0.728
0.646
0.673
0.688
0.699
0.707
0.714
0.720
0.724
0.729
0.649
0.675
0.689
0.700
0.708
0.715
0.720
0.725
0.729
0.653
0.676
0.691
0.701
0.709
0.715
0.721
0.725
0.729
0.656
0.678
0.692
0.702
0.710
0.716
0.721
0.726
0.730
0.659
0.680
0.693
0.703
0.710
0.716
0.722
0.726
0.730
0.661
0.681
0.694
0.703
0.711
0.717
0.722
0.727
0.730
0.664
0.683
0.695
0.704
0.712
0.718
0.723
0.727
0.731
0.666
0.684
0.696
0.705
0.712
0.718
0.723
0.727
0.731
SFS
at
122
°F
0
100
200
300
400
500
600
700
800
900
1000
2000
3000
0.732
0.755
0.769
0.735
0.757
0.770
0.738
0.759
0.771
0.741
0.760
0.772
0.743
0.761
0.773
0.746
0.763
0.773
0.748
0.764
0.775
0.750
0.764
0.775
0.752
0.766
0.776
0.754
0.767
0.777
4000
5000
6000
7000
8000
9000
0.778
0.784
0.790
0.795
0.798
0.802
Notes:
Values from this table are for 130 ºF, although the Saybolt Furol
seconds are at 122 ºF. This table alone must not be used for any
other temperatures. Values from this table may be used
interchangeably with values for kinematic and Saybolt Universal
viscosities if the latter are for 130 ºF.
For SFS at 210 ºF, assume SUS – 10 x SFS and use the Saybolt
Universal table.
Petroleum Refining – Chapter 13: Product Blending
23
Table 13.5: Flash Point Blending Index Numbers. Flash
Point,
°F
0
1
2
3
4
5
6
7
8
9
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240
250
260
270
280
290
168,000
86,600
46,000
25,200
14,200
8,240
4,890
2,970
1,840
1,170
753
495
331
224
154
108
76.3
54.7
39.7
29.1
21.6
16.1
12.2
9.31
7.16
5.56
4.35
3.43
2.72
2.17
157,000
81,200
43,300
23,800
13,500
7,810
4,650
2,830
1,760
1,120
722
475
318
216
149
104
73.8
52.9
38.4
28.2
20.9
15.7
11.9
9.07
6.98
5.42
4.24
3.35
2.66
2.12
147,000
76,100
40,700
22,400
12,700
7,410
4,420
2,700
1,680
1,070
692
456
305
305
144
101
71.4
51.3
37.3
27.4
20.3
15.2
11.6
8.83
6.80
5.29
4.14
3.27
2.60
2.08
137,000
71,400
38,300
21,200
12,000
7,030
4,200
2,570
1,600
1,020
662
438
294
200
138
97.1
69.0
49.6
36.1
26.6
19.7
14.8
11.2
8.60
6.63
5.16
4.04
3.19
2.54
2.03
128,000
67,000
36,100
20,000
11,400
6,670
4,000
2,450
1,530
978
635
420
283
193
134
93.8
66.7
48.0
35.0
25.8
19.2
14.4
10.9
8.37
6.47
5.03
3.95
3.12
2.48
1.99
120,000
62,900
34,000
18,900
10,800
6,330
3,800
2,330
1,460
935
609
404
272
186
129
90.6
64.5
46.5
33.9
25.0
18.6
14.0
10.6
8.16
6.30
4.91
3.86
3.05
2.43
1.95
112,000
59,000
32,000
17,800
10,200
6,010
3,620
2,230
1,400
896
584
388
261
179
124
87.5
62.4
45.1
32.9
24.3
18.1
13.6
10.4
7.95
6.15
4.79
3.76
2.98
2.37
1.90
105,000
55,400
30,100
16,800
9,680
5,700
3,441
2,120
1,340
857
560
372
252
172
120
84.6
60.4
43.6
31.9
23.6
17.6
13.3
10.1
7.74
5.99
4.68
3.68
2.91
2.32
1.86
98,600
52,100
28,400
15,900
9,170
5,420
3,280
2,020
1,280
821
537
358
242
166
116
81.7
58.4
42.3
30.9
22.9
17.1
12.9
9.82
7.55
5.84
4.56
3.59
2.85
2.27
1.82
92,400
49,000
26,800
15,000
8,690
5,150
3,120
1,930
1,220
786
515
344
233
160
112
79.0
56.5
40.9
30.0
22.2
16.6
12.5
9.56
7.85
5.70
4.45
3.51
2.78
2.22
1.79
Flash
Point,
°F
0
10
20
30
40
50
60
70
80
90
300
400
500
1.75
0.269
0.063
1.41
0.229
0.056
1.15
0.196
0.049
0.943
0.168
0.044
0.777
0.145
0.039
0.643
0.125
0.035
0.535
0.108
0.031
0.448
0.094
0.028
0.376
0.082
0.025
0.317
0.072
0.022
May be used to blend flash temperature, determined in any apparatus but, preferably, not to
blend closed cup with open cup determinations.
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
24
Table 13.6: Aniline Point Blending Index Numbers. Aniline Point, °F 0 -1 -2 -3 -4 -5 -6 -7 -8 -9
-10
0
20.0
49.1
17.4
46.0
14.9
42.8
12.6
39.8
10.3
36.8
8.10
33.8
6.06
30.9
4.17
28.1
2.46
25.3
1.00
22.6
Aniline Point, °F 0 1 2 3 4 5 6 7 8 9
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240
49.1
83.2
121
162
205
250
298
347
398
451
505
560
617
674
733
794
855
917
980
1,044
1,110
1,176
1,242
1,310
1,379
52.4
86.8
125
166
209
255
303
352
403
456
510
566
622
680
739
800
861
923
986
1,050
1,116
1,182
1,249
1,317
1,386
55.6
90.5
129
170
214
260
308
357
408
461
516
571
628
686
745
806
867
930
993
1,057
1,122
1,189
1,256
1,324
1,392
58.9
94.2
133
174
218
264
312
362
414
467
521
577
634
692
751
812
873
936
999
1,064
1,129
1,196
1,262
1,331
1,400
62.3
97.9
137
179
223
269
317
367
419
472
527
582
640
698
757
818
880
942
1,006
1,070
1,136
1,202
1,269
1,337
1,406
65.7
102
141
183
227
274
322
372
424
477
532
588
645
704
763
824
886
948
1,012
1,077
1,142
1,209
1,276
1,344
1,413
69.1
105
145
187
232
279
327
377
429
483
538
594
651
710
769
830
892
955
1,019
1,083
1,149
1,216
1,283
1,351
1,420
72.6
109
149
192
237
283
332
382
435
488
543
599
657
716
775
836
898
961
1,025
1,090
1,156
1,222
1,290
1,358
1,427
76.1
113
153
196
241
288
337
388
440
494
549
605
663
722
781
842
904
967
1,031
1,096
1,162
1,229
1,330
1,365
1,434
79.6
117
157
200
246
293
342
393
445
491
554
611
669
727
788
849
911
974
1,038
1,103
1,169
1,236
1,337
1,372
1,441
Mixed Aniline
Point, °F
0
1
2
3
4
5
6
7
8
9
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
-736
-668
-593
-511
-425
-334
-239
-140
-38.3
66.8
175
285
399
514
632
-730
-660
-584
-503
-416
-324
-229
-130
-27.9
77.4
186
297
410
526
644
-723
-653
-577
-494
-407
-315
-219
-120
-17.5
88.1
197
308
422
538
656
-716
-646
-569
-486
-398
-306
-210
-110
-7.06
98.8
208
319
433
550
668
-709
-639
-561
-477
-389
-296
-200
-100
3.39
110
219
330
445
561
680
-703
-631
-552
-468
-380
-287
-190
-89.6
13.9
120
230
342
456
573
692
-696
-623
-544
-460
-371
-277
-180
-79.4
24.4
131
241
353
468
585
704
-689
-616
-536
-451
-361
-267
-170
-69.2
35.0
142
252
364
479
597
716
-682
-608
-528
-442
-352
-258
-160
-58.9
45.5
153
263
376
491
609
728
-675
-600
-519
-433
-343
-248
-150
-48.6
56.1
164
274
387
503
620
741
Petroleum Refining – Chapter 13: Product Blending
25
Table 13.7: Pour Point Blending Indices for Distillate Stocks AST
M
50%
Temp
300
350
375
400
425
450
475
500
525
550
575
600
625
650
675
700
Pour
Point
70
65
60
55
50
45
40
35
30
25
20
15
10
5
0
-5
-10
-15
-20
-25
-30
-35
-40
-45
-50
-55
-60
-65
-70
133
114
99
88
72
60
52
44
37
32
27
23
20
17
14
12
10
8.8
7.5
6.4
5.5
4.6
4.0
3.3
2.8
2.5
2.1
1.8
1.5
131
111
94
79
68
56
48
41
34
29
24
20
17
15
12
10
8.8
7.4
6.3
5.3
4.5
3.7
3.2
2.7
2.3
1.9
1.6
1.4
1.1
129
109
92
77
66
54
46
39
32
27
23
19
16
14
11
9.5
8.0
6.8
5.7
4.7
4.0
3.3
2.8
2.4
2.0
1.7
1.4
1.2
0.99
128
107
90
75
63
52
44
37
31
26
21
18
15
13
10
8.7
7.3
6.1
5.1
4.2
3.6
2.9
2.5
2.1
1.7
1.4
1.2
1.0
0.84
127
105
87
73
61
50
42
35
29
24
20
17
14
12
9.6
8.0
6.6
5.5
4.6
3.7
3.2
2.6
2.2
1.8
1.5
1.2
1.0
0.85
0.71
125
103
85
71
59
48
40
33
27
23
19
16
13
11
8.7
7.2
5.9
4.9
4.1
3.3
2.8
2.3
1.9
1.5
1.3
1.1
0.87
0.72
0.60
123
101
82
68
56
46
38
32
26
21
17
14
12
9.7
7.9
6.5
5.3
4.4
3.6
2.9
2.4
2.0
1.6
1.3
1.1
0.90
0.74
0.60
0.50
120
98
80
66
54
44
36
30
24
20
16
13
11
8.8
7.1
5.8
4.7
3.9
3.2
2.5
2.1
1.7
1.4
1.1
0.93
0.77
0.62
0.50
0.42
118
96
77
63
52
42
34
28
23
18
15
12
9.8
7.9
6.3
5.1
4.1
3.4
2.8
2.2
1.8
1.4
1.2
0.98
0.78
0.65
0.52
0.41
0.36
115
94
74
61
49
40
32
26
21
17
14
11
8.8
7.1
5.6
4.5
3.6
3.0
2.4
1.9
1.5
1.2
1.0
0.82
0.66
0.55
0.43
0.34
0.30
113
91
72
58
47
38
30
24
19
15
12
10
8.0
6.3
5.0
3.9
3.2
2.6
2.1
1.7
1.3
1.0
0.86
0.68
0.56
0.46
0.36
0.28
0.25
110
88
69
56
44
35
28
23
18
14
11
9.0
7.1
5.6
4.4
3.4
2.8
2.2
1.8
1.4
1.1
0.90
0.73
0.58
0.47
0.37
0.30
0.23
0.20
108
85
67
53
42
33
26
21
16
13
10
8.1
6.3
5.0
3.8
3.0
2.5
1.9
1.5
1.2
0.96
0.75
0.62
0.48
0.38
0.30
0.24
0.18
0.15
105
82
64
50
39
31
24
19
15
12
9.1
7.2
5.6
4.4
3.4
2.7
2.2
1.7
1.3
1.0
0.80
0.62
0.51
0.38
0.31
0.24
0.19
0.14
0.11
103
79
62
48
37
29
22
18
14
11
8.3
6.4
5.0
3.8
3.0
2.4
1.9
1.4
1.1
0.90
0.67
0.51
0.41
0.31
0.25
0.19
0.14
0.10
0.08
100
76
60
46
35
27
21
16
13
10
7.5
5.8
4.5
3.5
2.7
2.1
1.6
1.2
0.94
0.72
0.56
0.43
0.33
0.25
0.20
0.15
0.10
0.07
0.05
From Gary & Handwerk
Online Blending
Because of limited storage space, many refineries today
(MAB refinery) use computer-controlled in-line blending
for blending gasoline and other products.
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
26
Inventories of blending stocks, together with cost and
physical property data are maintained in the computer.
When a certain volume of a given quality product is
specified, the computer uses linear programming models
to optimize the blending operations (select the optimum
volume of blending components) to produce the required
product at the lowest cost.
To ensure that the blended streams meet the desired
specifications, stream analyzers, such as boiling point,
specific gravity, RVP, and research and motor octane are
installed to provide feedback control of blending streams
and additives (if necessary).
Blending components to meet all critical specifications
most economically is a trial-and-error procedure which is
easily handled by a computer.
The large number of variables leads to a number of
equivalent solutions that give the approximate equivalent
total overall cost or profit.
Optimization programs (like PIMS for example) permit
the computer to provide the optimum blend to minimize
cost and maximize profit.
Both linear and nonlinear programming techniques are
used.
Nonlinear programming is preferred if sufficient data are
available to define the equations because components
blend non-linearly and values are functions of the
quantities of the components and their properties (specs).
Petroleum Refining – Chapter 13: Product Blending
27
Problems
1. Using values from Table 12.1, calculate the number of barrels of n-butane that have to
be added to a mixture of 1250 barrels of HSR gasoline, 750 barrels of LSR gasoline, and 620 barrels of C5 FCC gasoline to produce a 9 psi Reid vapor pressure. What are the research and motor octane numbers of the blend?
2. For the blend of components in problem 1, what would be the posted octane number of
the 9.0 psi RVP gasoline if 10 vol% MTBE was added to the gasoline mixture?
3. Calculate the amount of n-butane needed to produce a 12.5 psi RVP for a mixture of
2730 barrels of LSR gasoline, 2490 barrels of 94 RON reformate, 6100 barrels of heavy
hydrocrackate, and 3600 barrels of C5 + FCC gasoline. How much ETBE must be added
to produce a 90 RON product? Calculate the RVP of the final blend.
4. What is the flash point of a mixture of 2500 barrels of oil with a flashpoint of 120°F,
3750 barrels with a flashpoint of 35°F, and 5000 barrels with a 150°F flashpoint? 5. Calculate the pour point of the following mixture:
Component
Barrels ASTM
50%
temp., °F
Pour point,
°F
A 5,200 575 10 B 3,000 425 50 C 6,500 500 65 D 3,250 550 45
6. What is the viscosity of a blend of 2000 barrels of oil with a viscosity of 75.5 cSt at 130°F,
3000 barrels with 225 cSt at 130°F, and 5000 barrels with 6500 cSt at 130°F?
7. Calculate the octane numbers of the final blend and amount of n-butane needed for
producing a 9.5 psi RVP gasoline from 5100 BPSD of LSR gasoline, 3000 BPSD light
hydrocrackate, 4250 BPSD alkylate, 10,280 BPSD heavy hydrocrackate, 14,500 BPSD
FCC C5+ gasoline, 14,200 BPSD of 96 RON reformate, and 2500 BPSD of polymer
gasoline.
8. Recommend the best method for increasing the clear posted octane number of the pool
gasoline in problem 7 by 3 numbers. Estimate the cost involved. Assume any necessary
processing units are available and have the necessary capacity.
9. Calculate the number of barrels of n-butane that have to be added to a mixture of 1000
barrels of light thermal gasoline, 1000 barrels of polymer gasoline, and 1000 barrels of
C4= alkylate to produce a gasoline product having 10 psi Reid vapor pressure.
10. What is the posted octane number and Reid vapor pressure of the gasoline product of
problem 3?
11. Calculate the clear octane numbers (RON and MON) and the amount of butane needed
for a 12.0 psi RVP gasoline produced from the following:
BPSD
LSR naphtha 4,200 Light hydrocrackate 1,800 C5+ alkylate 4,500
Copyrights © 2001 – 2014, Dr. Tareq Albahri, Chem. Eng. Dept., Kuwait University
28
Heavy hydrocrackate 9,150 Reformate (94 RON) 11,500 C5+ FCC gasoline 15,600
12. Recommend the best method (lowest capital cost) for increasing the posted octane
number of the pool gasoline in problem 11 by 5.5 octane numbers. Estimate the size of
the unit and its 1994 construction cost.
HW solve problems 3, 5, 6, 10