Crude Oil Distillation

CRUDE OIL DISTILLATION The feed to a refinery often changes every few days. An existing refinery has received an Indonesian crude oil and you must simulate the atmospheric distillation column to establish the correct operating conditions for a throughput of 120,000 barrels/day. The crude unit configuration and typical operating data are shown in Figure R3.1. The products must meet the specified D86 and TBP points in Table R3.1, and the yields are to be calculated.

Figure R3.1 Crude Distillation Column

Table R3.1 ASTM D86 (F) LV %

Kerosene

Diesel

Gas Oil

Topped Crude -

0

-

330

460

555

5

-

380

530

635

520

665

95 100 *

Naphtha

340 370

550

705

*

(695) *

(885)

*

(955)

-

Figures in parentheses are TBP points rather than ASTM.

Process Data

For this simulation, the stripping stream and pumparound cooling shown on Figure

R3.1 are used. The crude oil has been analysed as an atmospheric TBP curve and defined lightend components as shown in Table R3.2. Table R3.2 CRUDE OIL DATA TBP @ 760 mm Hg LV%

Temp (F)

LV%

Lightends Temp (F)

Component

LV%

5

149

50

690

Ethane

0.1

10

208

60

770

Propane

0.2

20

330

70

865

i-Butane

0.3

30

459

80

980

n-Butane

0.7

40

590

100

i-Pentane

0.5

n-Pentane

1.2

Total

3.0

Average API gravity

29.2

1600

The laboratory data for the TBP curve are supplied only up to the 80% point. A typical value is assumed for the 100% point to assist the extrapolation of the curve.

Methods and Data

The GS thermodynamic system is recommended for calculating K-values and enthalpies in crude and vacuum systems. The BK10 system may also be used, but it tends to predict slightly less vaporization. Column temperatures can generally be matched with either system. If not, the column pressure data are probably in error. Accurate characterization of the crude oil is vital for good simulation results. The greatest errors often appear in the residue stream and can lead to poor results when simulating the downstream vacuum column. The characterization may be improved by supplying gravity and molecular weight data if they are available.

The program automatically generates a number of petroleum fractions and calculates the molecular weight, gravity, and boiling point for each. These are then used in standard petroleum correlations to generate all the other required properties.

Simulation Model (Shortcut)

Viscosity and thermal conductivity data are generated for the streams for use in other calculations. The API data book method is selected for the liquid viscosities. For crude oil streams, these data are more accurate than the ’PETRO’ option used for the other transport properties. The first step in the simulation is to ensure that it is possible to produce the specified products from the crude oil feed and establish the material balance. The multidraw shortcut distillation model (MODEL = REFINE) is a quick and easy tool for these calculations. This model uses the Fenske calculation method and considers the column to be a series of two-product columns as shown in Figure R3.2. The condenser is simulated with an external flash drum. The specifications chosen for the shortcut model define the separation in each section. For this simulation, the 95% distillation points and 5-95% gaps are used. The data are taken from Table R3.1. 5% and 95% points should always be used instead of initial and end points, as they are generally more accurate. The simulated end points are affected by the number of petroleum cuts, the parameter TBPEP (on the ASSAY statement in Component Data) which defaults to 98%, and the Fenske model itself, which tends to overfrac- tionate on the product tails. In addition, the shortcut simulation ignores the sidestrippers which also affect the ends of the curves.

Figure R3.2 Shortcut Crude Unit Model

In the shortcut model, all the stripping steam is added with the feed. The main effect of this on the simulation results is that the influence of the steam on the product temperatures is not modeled, and the calculated temperatures will be high.

Input Data (Shortcut)

The simulation units are defined as English but with pressure as psig and liquid volumes in barrels. As crude oil has no defined components, the component flow rate output is suppressed, and only the stream summary is printed. The PRINT TBP option gives the TBP and ASTM curves for all hydrocarbon streams. It is not known whether or not there will be any vapor product from the column. As there may be vapor, the condenser is defined as mixed phase at the defined temperature. The MODEL=REFINE option specifies no reflux between sections in the column. The default would assume total reflux between the sections. The product rate estimates are supplied as volume percent cutpoints on the crude oil feed.

Input Data File: TITLE

PROBLEM=R 3S,PROJEC T=APPBR IEFS,USER =SIMSCI, DATE=SE PT 90

DIMEN

PRESS=PSIG,LIQV=BBL

PRINT

STREAM=SUMMARY,TBP

COMPONENT DATA LI BID

1 ,H2 O/ 2, C2 /3,C3 /4,IC4/5,NC4/6,IC5/7,NC5

THERMODYNAMIC DATA METHODS SYSTEM=GS,COND=PETR,VISC(V)=PETR,VISC(L)=API STREAM DATA PROP STREAM=1,TEMP=450,PRES=14,RATE(V)=5000,ASSAY=LV TBP

STREAM=1,PRES(MMHG)=760,&

DATA=3,97/5,149/10,208/20,330/30,459/40,590/& 50,690/60,770/70,865/80,980/100,1600 A PI

S TR EA M= 1, AV G= 29 .2

LIGHT STREAM=1,PERCENT(V)=3,& COMP(V)=2,0.1/3,0.2/4,0.3/5,0.7/6,0.5/7,1.2 PROP STREAM=WATR,TEMP=600,PRES=60,PHASE=V,COMP(W)=20000 NAME 1,CRUDE FEED/9,NAPHTHA/10,KEROSENE/11,DIESEL/& 12,GAS OIL/20,T OPPED CRUDE UNIT OPERATIONS SHORTCUT UID=SC0 1,NAME=CR UDE TOWER FEED

1,WATR

PROD

STREAM=89,PHASE=M,PRESS=8.5,CUTP(V)=25

PROD

STREAM=10,PHASE=L,CUTP(V)=40,PRES=11.8

PROD


PROD


PROD

STREAM=20,PHASE=L,PRES=14.4

COND

TYPE=MIXED,TEMP=110

EVAL

MODEL= REFINE

SPEC

STREAM=89,D86(95),VALUE=340

SPEC

STREAM=10,D86(5),DIFF,STREAM=89,D86(95),VALUE=40

SPEC


SPEC

STREAM=11,D86(5),DIFF,STREAM=10,D86(95),VALUE=10

SPEC


SPEC

STREAM=12,D86(5),DIFF,STREAM=11,D86(95),VALUE=-30

SPEC

STREAM=12,TBP(95),VALUE=885

SPEC

STREAM=20,TBP(5),VALUE=695 FLASH

UID=FL0 1,NAME=C ONDENSER FEED 89

PROD

V=8,L=9,W=7

ISO

TEMP=110,PRES= 5.3

END

Output (Shortcut)

The shortcut column results are shown on the next page. The shortcut model predicts the minimum number of trays, calculated at total reflux, needed to meet the specified separations. Typical values for crude oil separations for each column section are shown in Table R3.3.

Table R3.3 TYPICAL SHORTCUT TRAYS Column Section

Minimum Trays

Naphtha - Kerosene

3.5 - 5.0

Kerosene - Diesel

2.5 - 3.5

Diesel - Gas oil

2.0 - 3.0

Gas oil -Topped crude

1.3 - 1.8

As long as the shortcut model reports figures within these ranges, the separations will be feasible. Significant departures from these values mean a difficult, if not impossible, separation. The simulation predicted no overhead vapor at the desired condenser conditions. This is not unusual for crude unit simulations because some lightends may have been lost in sampling the crude oil, or because lightends produced by cracking in the furnace are not included in the simulation model. Once the shortcut model is solved, the material balance is defined. If difficulties occur solving the rigorous model, then the heat balance is likely to be at fault.

SHORTCUT COLUMN OUTPUT UNIT 1, ’SC01’, ’CRUDE TOWER’ FEEDS STREAM PHASE ------------ -----------1 WATR

MIXED VAPOR

PRODUCTS STREAM

PHASE

-------------------- MATERIAL BALANCES -------------------SECTION NO OF LB-MOL/HR LB/HR BBL/HR TRAYS ------------ ------------ --------------------------------------------------------------------------------------------- --------89 MIXED 2878.68 279901.38 1090.22 1 4.49 WATER

1105.36

19913.15

10

LIQUID

1047.10

184786.42

641.70

2

3.73

11

LIQUID

574.76

144886.42

477.04

3

2.76

12

LIQUID

715.23

236618.47

747.78

4

1.43

20

LIQUID

1337.39

695517.88

2043.50

TOTALS

7658.53

1561623.7

56.89

5057.14

12.41

SPECIFICATIONS PARAMETER TYPE -----------------------------------STRM STRM STRM STRM STRM STRM STRM STRM

COMP. SPECIFICATION SPECIFIED CALCULATED NO TYPE VALUE VALUE ------------- ------------------------- -------------------89 10 10 11 11 12 12 20

D86 D86 D86 D86 D86 D86 TBP TBP

95 PCT 5 PCT 95 PCT 5 PCT 95 PCT 5 PCT 95 PCT 5 PCT

3.400E+02 4.000E+01 5.200E+02 1.000E+01 6.650E+02 -3.000E+01 8.850E+02 6.950E+02

3.400E+02 4.000E+01 5.200E+02 9.999E+00 6.650E+02 -3.001E+01 8.850E+02 6.950E+02

Simulation Model (Rigorous)

The number of theoretical trays must be established for the rigorous distillation. This may be obtained by:

- applying typical overall tray efficiencies to the number of actual trays - using values from previous simulations of the column - assuming that the number of theoretical trays is about twice the minimum number In this example, typical efficiencies were used to get the configuration of the model shown in Figure R3.3.

Figure R3.3 Rigorous Crude Unit Model

Virtually all the heat in the distillation enters with the crude oil feed, and so it is vital that the feed temperature is correct. For this reason, the furnace and flash zone are included in the simulation as a heat source on the feed tray. The feed is specified as liquid at the flash zone pressure to ensure that no flash is performed and all the feed is placed on this tray. The furnace duty is then calculated to match the specified liquid runback into the flash zone. Only one other specification can be made on the main column, together with one on each sidestripper, and so not all the distillation specifications on the shortcut can be used. The best strategy is to specify one distillation point or gap for each product, except for the topped crude. The topped crude is not usually specified since this has the greatest uncertainty. Specifying the 95% points generally gives good results. If large differences appear at the top of the curves, then the simulation may be improved by specifying some 5% points. The specification variables are the condenser duty and the side product draw rates. As for the shortcut simulation, 5% and 95% points are used in preference to initial and end points. The circulation rates for the pumparound cooler circuits are calculated to meet the desired cooling duties and return temperatures. When specifying sidecooler duties, be wary of duties which are based on measured pumparound rates. These are notoriously inaccurate, and too much cooling will dry up the liquid leaving the tray above the cooler. The subsequent calculation failure reflects the operational failure of the actual column when drying up occurs. If pumparound duties are uncertain, they may be calculated to meet specified liquid runbacks. The shortcut model showed that there is no overhead vapor. Therefore, the condenser is defined as TYPE = TFIX, which is total at a fixed temperature. Solution of the main column is enhanced by using the molal product flows determined in the shortcut simulation as initial estimates. The REFINERY model is used to generate the initial solution profiles The temperature of the oil leaving the furnace is not the same as the flash zone temperature. In order to calculate the furnace temperature, a flash is used to add the calculated furnace duty to the feed stream.

Input Data (Rigorous)

The dimensional units and printout options for the rigorous simulation are the same as were used in the shortcut model. The steam feeds are now fed to the bottom of the main column and to the sidestrippers. The column is defined as a refinery unit, and a damping factor of 0.8 is automatically applied to the IO solution method. This damping assists in the convergence of this type of column. The sidestrippers are entered as separate units, but PRO/II solves them simultaneously with the main column. The column feed temperature is not calculated until after the column has been converged

Input Data File: TITLE

PROBLEM=R3R,PROJECT=APPBRIEFS,USER=SIMSCI,DATE=SEP T 90

DIMEN

PRES=PSIG,LIQV=BBL

PRIN T

STREAM= SUMMARY, TBP COMPONE NT DATA LIBID

1,H2O/2,C2/3,C3/4,IC4/5,NC4/6,IC5/7,NC5

THERMOD YNAMIC DATA METHODS SYSTEM=GS,COND=PETR,VISC(V)=PETR,VISC(L)=API STREA M DATA PROP STREAM=1,TEMP=450,PRES=14,PHASE=L,RATE(V)=5000,ASSAY=LV TB P STREAM=1,PRES(MMHG)=760,& DATA=3,97/5,149/10,208/20,330/30,459/40,590/& 50,690/60,770/70,865/80,980/100,1600 API

STREAM=1,AVG=29.2

LIGHT STREAM=1,PERCENT(V)=3,& COMP(V)=2,0.1/3,0.2/4,0.3/5,0.7/6,0.5/7,1.2 PROP STREAM=2,TEMP=600,PRES=60,PHASE=V,RATE(W)=10000,& COMP=1,100 PROP STREAM=3,TEMP=600,PRES=60,PHASE=V,RATE(W)=1500,& COMP=1,100 PROP STREAM=4,TEMP=600,PRES=60,PHASE=V,RATE(W)=4500,& COMP=1,100 PROP STREAM=5,TEMP=600,PRES=60,PHASE=V,RATE(W)=4000,& COMP=1,100 NAME 1,CRUDE FEED/9,NAPHTHA/10,KEROSENE/11,DIESEL/& 12,GAS OIL/20,TOPPED CRUDE UNIT OPERATIONS COLUMN PARAM

UID=COL1,NAME=CRUDE TOWER TRAY=20,DAMP=0.8

FEED

1,18/ 2,20/ 18,15/ 16,11/ 14,7

COND

TYPE=TFIX,TEMP=110

PROD

OVHD=9,2879,WATER=7,1,1105,BTMS=20,&

LDRAW=15,8,1047/17,12,575/19,16,715 DUTY

1,1/2,18/3,13,-40/4,9,-50/5,2,-50

VARY

DUTY=1,2

PA

FROM=14,TO=13,PHASE=L,TEMP=450

PA


PA


PRESS

1,5.3/2,8.5/18,12.5/20,13.0

ESTI

MODEL=REFINERY

SPEC

COLUMN=COL1,TRAY=17,PHASE=L,RATE(V),RATIO,&

STREAM=1,VALUE=0.03 SPEC


SIDESTRIPPER UID=SS01, NAME=KERO STRIP PARAM FEED 15,1/ 5,2 PROD PSPEC

TRAY=2

OVHD=14,BTMS=10,1047 TOP=11.8

SPEC


VARY

FEED=15

SIDESTRIPPER UID=SS02, NAME=DIES EL STRIP PARAM

TRAY=2

FEED

17,1/ 4,2

PROD

OVHD=16,BTMS=11,575

PSPEC

TOP=12.5

SPEC


VARY

FEED=17

SIDESTRIPPER UID=SS03, NAME=AGO STRIP PARAM FEED

19,1/ 3,2

PROD PSPEC

TRAY=2

OVHD=18, BTMS=12,715 TOP=13.3

SPEC

STREAM=12,TBP(95),VALUE=885

VARY

FEED=19

FLASH

UID=FL1,NAME=FEED T EM P FE ED

PROD

1

M=1A

DEFINE PRES AS COLUMN=C OL1,TRAY =18,PRES DEFINE DUTY AS COLUMN=COL1,DUTY(2) END

COMPARISON OF SHORTCUT AND RIGOROUS RESULTS

The product qualities are compared below: ASTM D86 (F) Naphtha

Kerosene

Diesel

Gas Oil

LV%

S/C

Rig

S/C

Rig

S/C

Rig

S/C

Rig

0 5

Bbl/hr

-52 78 130 218 314 340 376 1090

-52 78 130 218 315 340 367 1083

358 380 389 433 500 520 559 642

304 374 390 431 499 520 562 612

510 530 537 585 646 665 700 477

450 513 528 585 648 665 696 525

596 635 646 715 816 842 890 798

490 613 639 717 817 842 884 699

API

61.5

61.5

40.6

40.7

31.6

31.8

25.1

25.2

10 50 90 95 100

TBP @ 760 mm Hg (F) Gas Oil

Topped Crude

LV%

S/C

Rig

S/C

Rig

0 5

Bbl/hr

520 611 637 727 850 885 949 748

422 593 630 728 851 885 942 699

463 695 747 972 1447 1523 1548 2043

548 695 743 968 1445 1522 1548 2071

API

25.1

25.2

14.1

14.1

10 50 90 95 100

There is good agreement between the 5% and 95% points, especially towards the top of the column. The fractionation on the product front ends (0-5%) is sharper with the shortcut model, while the rigorous simulation predicts better fractionation on the tail ends (95-100%). This is largely due to the simplifying assumptions of the shortcut model and the presence of the sidestrippers in the rigorous simulation. Because of the simplification in the way the steam feeds are handled in the shortcut model, the product temperatures will not match. The rigorous values should always be used.

Results The simulation shows that the column can be operated to produce the required products. The yield of each product is shown in the output. The pumparound rates, furnace and condenser duties have also been calculated along with the actual temperature of the oil leaving the furnace. The flash output below shows that the furnace outlet temperature is 694.5 F, while the column output shows that the flash zone is at 692.9 F.

Output (Rigorous)

The column summaries show the output for the main column and the sidestrippers. Tables may also be produced with vapor and liquid rates, densities and transport properties, but these are not presented here. The stream component output was suppressed and only the stream summaries are printed. A sample of the stream summary is show for both wet and dry basis properties. Part of the distillation curve output is shown for the feed and some product streams. All pure water streams are omitted from this output. Finally, a comparison is presented of the analyses of the shortcut and rigorous products.

FEED TEMPERATURE FLASH FLASH ID NAME FEEDS PRODUCTS MIXED TEMPERATURE, F PRESSURE, PSIG PRESSURE DROP, PSI MOLE FRAC VAPOR MOLE FRAC TOTAL LIQUID MOLE FRAC H/C LIQUID MOLE FRAC FREE WATER DUTY, MM BTU/HR FLASH TYPE

FL1 FEED TEMP 1 1A 695.117 12.500 1.500 0.77043 0.22957 0.22957 0.00000 291.79562 ADIABATIC-P

CRUDE COLUMN SUMMARY UNIT 1, ’COL1’, ’CRUDE TOWER’ TOTAL NUMBER OF ITERATIONS IN/OUT METHOD

14

COLUMN SUMMARY -

--

--

--

--

-

DEG F -

--

--

-

-

-

--

--

--

--

--

NET FLOW RATES LIQUID VAPOR PSIG -

--

-

--

--

-

--

1 1077.6W 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20

---

---

--

--

--

-

--

--

--

FEED -

--

--

HEATER TRAY PRODUCT DUTIES LB-MOL/HR

--

- -

--

--

--

TEMP

PRESSURE MM BTU/HR

- -

--

--

--

--

--

110.0

5.30

2424.1

274.3 311.4 339.1 355.3 368.6 383.7 406.1 438.6 471.1 503.9 533.0 562.7 592.8 619.5 642.8 673.5 693.5 690.2 684.4

8.50 8.75 9.00 9.25 9.50 9.75 10.00 10.25 10.50 10.75 11.00 11.25 11.50 11.75 12.00 12.25 12.50 12.75 13.00

9778.5 5091.8 5017.3 4849.2 4573.5 4122.9 2284.7 6078.8 3374.3 2947.3 1664.0 3871.8 2170.2 1806.0 486.2 132.6 1598.0 1477.6

2875.9L 6377.6 8713.7 9045.3 8970.8 8802.6 8527.0 7618.6 7028.5 8300.2 8118.1 7254.0 6800.0 7455.4 7306.2 6777.1 6228.8 5875.2 792.3 671.8

-50.0000

457.8V 1248.2L -50.0000 437.2V 829.4L -40.0000 164.9V 771.5L 6548.3M 555.1V

291.7956 1360.9L

SIDESTRIPPER SS01 1/ 21

392.0

11.80

1139.5

2/ 22

377.0

11.80

1/ 23 2/ 24

519.5 503.9

12.50 12.50

740.8

1/ 25 2/ 26

639.4 633.3

13.30 13.30

736.8

349.1

-135.2194

1248.2L

457.8V

222.0V

1012.4L

SIDESTRIPPER SS02

348.6

829.4L 249.8V

437.2V 642.0L

130.2

771.5L 83.3V

164.9V 689.8L

SIDESTRIPPER SS03

CRUDE COLUMN SUMMARY (Cont) UNIT 1, ’COL1’, ’CRUDE TOWER’ TYPE

-

--

--

--

-

--

--

--

-

--

--

(CONT) FEED AND PRODUCT STREAMS

STREAM

--

-

-

--

PHASE

--

-

FROM TRAY -

--

TO TRAY -

-

LIQUID FRACTION

--

-

-

FLOW RATES LB-MOL/HR

--

--

--

-

-

HEAT RATES MM BTU/HR --

--

--

--

--

--

FEED FEED FEED FEED FEED PRODUCT PRODUCT PRODUCT PRODUCT PRODUCT PRODUCT

14 16 18 1 2 9 7 15 17 19 20

VAPOR VAPOR VAPOR MIXED VAPOR LIQUID WATER LIQUID LIQUID LIQUID LIQUID

15 5 14 10

LIQUID VAPOR VAPOR LIQUID

FEED FEED PRODUCT PRODUCT

17 4 16 11


FEED FEED PRODUCT PRODUCT

19 3 18 12


7 11 15 18 20

0.0000 0.0000 0.0000 0.5778 0.0000

457.82 437.20 164.95 6548.34 555.09 2875.90 1077.59 1248.19 829.36 771.50 1360.87

14.5426 18.6622 9.8699 326.2005 13.3040 3.4362 1.5132 35.8340 49.0964 78.1636 231.1219

21 22

1.0000 0.0000

1248.19 222.04 457.82 1012.40

35.8340 5.3216 14.5426 26.6130

23 24

1.0000 0.0000

829.36 249.79 437.20 641.96

49.0964 5.9868 18.6622 36.4206

25 26

1.0000 0.0000

771.50 83.26 164.95 689.81

78.1636 1.9956 9.8699 70.2886

1 1 8 12 16 20

SIDESTRIPPER SS01 FEED FEED PRODUCT PRODUCT

21 22

SIDESTRIPPER SS02

23 24

SIDESTRIPPER SS03

25 26

OVERALL MASS BALANCE, (FEEDS - PRODUCTS) OVERALL HEAT BALANCE, (H(IN) - H(OUT) )

1.8405E-03 -8.6010E-03

PUMPAROUNDS TRAY -

--

TEMP, DEG F --

FROM

TO

-

--

- -

-

--

--

--

--

--

FROM ---

--

-

--

- -

LIQUID FRACTION

-

--

--

--

--

--

-

RATES

--

--

--

--

--

14 13 10 9 3 2

--

--

TO --

--

FROM -

--

TO

--

--

-

LB-MOL/HR --

--

--

M LB/HR -

--

--

STD BBL/HR --

--

-

--

592.8 471.1 311.4

450.0 310.0 175.0

1.0000 1.0000 1.0000

1.0000 1.0000 1.0000

1552.37 2522.48 5018.31

422.898 505.309 654.301

1374.45 1719.86 2385.77

-

UNIT 1, ’COL1’, ’CRUDE TOWER’

(CONT) SPECIFICATIONS

PARAMETER TYPE

COMP NO

TRAY

-

--

--

--

--

-

--

--

--

--

-

--

-

-

TRAY LIQ STRM STRM STRM STRM

9 10 11 12

--

--

17 1 22 24 26

SPECIFICATION SPECIFIED NO TYPE VALUE -

-

D86 D86 D86 TBP

--

--

--

--

VOL RATIO 95 PCT 95 PCT 95 PCT 95 PCT

--

--

-

CALCULATED VALUE --

3.000E-02 3.400E+02 5.200E+02 6.650E+02 8.850E+02

--

--

--

-

3.002E-02 3.400E+02 5.200E+02 6.651E+02 8.851E+02

PRODUCT STREAM SUMMARY STREAM ID NAME PHASE

10 KEROSENE WET LIQUID

--------- TOTAL STREAM --------RATE, LB-MOL/HR M LB/HR TEMPERATURE, F PRESSURE, PSIG MOLECULAR WEIGHT ENTHALPY, MM BTU/HR

11 DIESEL WET LIQUID

12 GAS OIL WET LIQUID

WET VAPOR

1012.402 175.903 377.003 11.800 173.748 26.613

641.956 158.610 503.923 12.500 247.073 36.421

689.814 224.796 633.265 13.300 325.880 70.289

457.823 39.007 391.983 11.800 85.202 14.543

151.294 1.00000 0.00000

229.623 1.00000 0.00000

312.677 1.00000 0.00000

372.817 0.00000 0.00000

N/A

N/A

457.823 39.007 154.537 173.735 85.202 372.817 0.537 252.414 0.01652 0.01088

N/A

BTU/LB MOLE FRACTION LIQUID MOLE FRACTION FREE WATER --------- TOTAL VAPOR -----------RATE, LB-MOL/HR M LB/HR M FT3/HR STD VAP RATE(1), M FT3/HR MOLECULAR WEIGHT ENTHALPY, BTU/LB CP, BTU/LB-F DENSITY, LB/M FT3 THERMAL COND, BTU/HR-FT-F VISCOSITY, CP --------- TOTAL LIQUID RATE, LB-MOL/HR

N/A N/A N/A N/A N/A N/A N/A

N/A N/A N/A N/A N/A N/A N/A

N/A N/A N/A N/A N/A N/A N/A N/A N/A N/A

1012.402

641.956

689.814

158.610 645.271 451.688 523.015 247.073 229.623 0.657 245.804 0.04356 0.27529

224.796 917.344 642.139 711.077 325.880 312.677 0.707 245.051 0.03833 0.27323

N/A N/A

N/A N/A

14

---------

M LB/HR 175.903 BBL/HR 724.057 GAL/MIN 506.838 STD LIQ RATE, BBL/HR 611.476 MOLECULAR WEIGHT 173.748 ENTHALPY, BTU/LB 151.294 CP, BTU/LB-F 0.614 DENSITY, LB/BBL 242.941 TH COND, BTU/HR-FT-F 0.05023 VISCOSITY, CP 0.27647

(1) STD VAPOR VOLUME IS 379.48 FT3/LB-MOLE (60 F AND 14.696 PSIA)


PRODUCT STREAM SUMMARY (Cont) STREAM ID

10 NAME PHASE

KEROSENE WET LIQUID

------------ DRY STREAM -----------RATE, LB-MOL/HR M LB/HR STD LIQ RATE, BBL/HR MOLECULAR WEIGHT MOLE FRACTION LIQUID REDUCED TEMP (KAYS RULE)

SPECIFIC GRAVITY API GRAVITY

1004.161 175.754 611.052 175.026 1.0000 0.6824

11 12 14 DIESEL GAS OIL WET LIQUID WET LIQUID WET VAPOR

636.901 158.519 522.755 248.891 1.0000 0.7001

685.516 224.719 710.856 327.810 1.0000 0.7293

242.392 35.126 125.822 144.916 0.0000 0.7465

PRES (KAYS RULE) 0.0807 0.1096 0.1439 0.0704 ACENTRIC FACTOR 0.5145 0.6311 0.7448 0.4487 WATSON K (UOPK) 11.733 11.732 11.732 11.744 STD LIQ DENSITY, LB/BBL 287.626 303.238 316.124 279.177 0.8214 0.8660 0.9028 0.7973 40.765 31.896 25.235 45.978

------------ DRY VAPOR RATE, LB-MOL/HR

-------------

N/A N/A N/A N/A N/A N/A N/A N/A


242.392 35.126 80.545 91.983 5.003 144.916 0.9695 0.544 436.106 0.01532 0.00920

------------ DRY LIQUID RATE, LB-MOL/HR 1004.161 M LB/HR 175.754 BBL/HR 723.572 GAL/MIN 506.499

636.901 158.519 644.938 451.455

685.516 224.719 916.993 641.893

N/A N/A N/A N/A

STD LIQ RATE, BBL/HR SPECIFIC GRAVITY (H2O=1.0) MOLECULAR WEIGHT Z (FROM K) CP, BTU/LB-F DENSITY, LB/BBL THERMAL COND, BTU/HR-FT-F VISCOSITY, CP

522.755 0.8660 248.891 0.0000 0.657 245.790 0.04355 0.27714

710.856 0.9028 327.810 0.0000 0.707 245.061 0.03832 0.27494


M LB/HR N/A M FT3/HR N/A STD VAP RATE(1), M FT3/HR SPECIFIC GRAVITY (AIR=1.0) MOLECULAR WEIGHT Z (FROM K) CP, BTU/LB-F DENSITY, LB/M FT3 THERMAL COND, BTU/HR-FT-F VISCOSITY, CP

N/A


611.052 0.8214 175.026 0.0000 0.614 242.898 0.05020 0.27786

N/A N/A N/A

(1) STD VAPOR VOLUME IS 379.48 FT3/LB-MOLE (60 F AND 14.696 PSIA)

N/A

PRODUCT DISTILLATION CURVES STREAM ID NAME

1 CRUDE FEED

1A

9 NAPHTHA

10 KEROSENE

0 LV PERCENT 5 147.566 10 208.225 30 459.057 50 689.818 70 864.505 90 1240.591 95 1414.367 100 1547.776

-5.793

-5.793 147.566 208.225 459.057 689.818 864.505 1240.591 1414.367 1547.776

-82.191 42.967 93.091 171.290 217.790 269.335 331.246 352.148 375.169

242.064 340.412 360.880 401.007 434.658 471.151 520.628 542.111 583.764

0 LV PERCENT -20.472 26.235 225.327 417.429 568.937 914.411 1083.646 1218.001

-136.159

-136.159 -20.472 26.235 225.327 417.429 568.937 914.411 1083.646 1218.001

-192.547 -99.743 -61.953 -2.270 33.649 73.844 122.659 139.273 157.650

52.528 129.936 146.234 178.376 205.527 235.176 275.718 293.447 328.038

0 LV PERCENT 29.766 5 181.851 10 242.008 30 465.239 50 679.107 70 834.151 90 1192.319 95 1334.165 100 1443.061

29.766 181.851 242.008 465.239 679.107 834.151 1192.319 1334.165 1443.061

-52.478 77.957 130.195 185.348 217.630 262.078 315.191 340.009 367.342

296.427 372.104 387.854 409.109 430.172 456.923 498.497 520.046 561.824

0 LV PERCENT -22.476 5 140.822 10 205.329 30 457.986 50 689.818 70 864.505 90 1240.591 95 1414.367 100 1547.776

-22.476 140.822 205.329 457.986 689.818 864.505 1240.591 1414.367 1547.776

-41.402 67.857 111.705 179.475 217.790 269.335 331.246 352.148 375.169

297.840 361.443 374.735 407.476 434.658 471.151 520.628 542.111 583.764

29.766 181.851 242.008 465.239 648.793 746.392 866.448 895.100 918.582

-52.478 77.957 130.195 185.348 217.630 262.078 315.191 340.009 367.342

296.427 372.104 387.854 409.109 430.172 456.923 492.943 513.127 551.333

TBP AT 760 MM HG

TBP AT

10 MM HG

5 10 30 50 70 90 95 100 ASTM D86

ASTM D1160

ASTM D86 WITH CRACKING 0 LV PERCENT 29.766 5 181.851 10 242.008 30 465.239 50 648.793 70 746.392 90 866.448 95 895.100 100 918.582

Crude Oil Distillation

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