21
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

Crude Oil Distillation

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Page 1: Crude Oil Distillation

CRUDE OIL DISTILLATIONThe 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

Page 2: Crude Oil Distillation

Table R3.1ASTM D86 (F)

LV % Naphtha Kerosene Diesel Gas Oil ToppedCrude

0

5

95

100

-

-

340

370

330

380

520

550

460

530

665

705

555

635

(885)*

(955)*

-

(695)*

-

-

* Figures in parentheses are TBP points rather than ASTM.

Process Data For this simulation, the stripping stream and pumparound cooling shown on FigureR3.1 are used.

The crude oil has been analysed as an atmospheric TBP curve and defined lightend components as shown in Table R3.2.

Table R3.2CRUDE OIL DATA

TBP @ 760 mm Hg Lightends

LV% Temp (F) LV% Temp (F) Component LV%

5

10

20

30

40

149

208

330

459

590

50

60

70

80

100

690

770

865

980

1600

Ethane

Propane

i-Butane

n-Butane

i-Pentane

n-Pentane

0.1

0.2

0.3

0.7

0.5

1.2

Average API gravity 29.2 Total 3.0

Methods and Data

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

The GS thermodynamic system is recommended for calculating K-values and enthalpies in crude and vacuum systems. The BK10 system may also be used, butit 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 calcu-lates the molecular weight, gravity, and boiling point for each. These are then usedin standard petroleum correlations to generate all the other required properties.

Page 3: Crude Oil Distillation

SimulationModel(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 numberof 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 side- strippers which also affect the ends of the curves.

Figure R3.2

Shortcut Crude Unit Model

Page 4: Crude Oil Distillation

Input Data(Shortcut)

In the shortcut model, all the stripping steam is added with the feed. The main effectof 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.

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=R3S,PROJECT=APPBRIEFS,USER=SIMSCI,DATE=SEPT 90DIMEN PRESS=PSIG,LIQV=BBL PRINT STREAM=SUMMARY,TBP COMPONENT DATALIBID 1,H2O/2,C2 /3,C3 /4,IC4/5,NC4/6,IC5/7,NC5THERMODYNAMIC DATAMETHODS SYSTEM=GS,COND=PETR,VISC(V)=PETR,VISC(L)=API STREAM DATAPROP 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

API STREAM=1,AVG=29.2LIGHT STREAM=1,PERCENT(V)=3,& COMP(V)=2,0.1/3,0.2/4,0.3/5,0.7/6,0.5/7,1.2PROP STREAM=WATR,TEMP=600,PRES=60,PHASE=V,COMP(W)=20000NAME 1,CRUDE FEED/9,NAPHTHA/10,KEROSENE/11,DIESEL/&12,GAS OIL/20,TOPPED CRUDE UNIT OPERATIONSSHORTCUT UID=SC01,NAME=CRUDE TOWER FEED 1,WATRPROD STREAM=89,PHASE=M,PRESS=8.5,CUTP(V)=25PROD STREAM=10,PHASE=L,CUTP(V)=40,PRES=11.8PROD STREAM=11,PHASE=L,CUTP(V)=55,PRES=12.5PROD STREAM=12,PHASE=L,CUTP(V)=75,PRES=13.3PROD STREAM=20,PHASE=L,PRES=14.4COND TYPE=MIXED,TEMP=110EVAL MODEL= REFINE

Page 5: Crude Oil Distillation

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

SPEC STREAM=10,D86(5),DIFF,STREAM=89,D86(95),VALUE=40SPEC STREAM=10,D86(95),VALUE=520SPEC STREAM=11,D86(5),DIFF,STREAM=10,D86(95),VALUE=10SPEC STREAM=11,D86(95),VALUE=665SPEC STREAM=12,D86(5),DIFF,STREAM=11,D86(95),VALUE=-30SPEC STREAM=12,TBP(95),VALUE=885SPEC STREAM=20,TBP(5),VALUE=695

FLASH UID=FL01,NAME=CONDENSER FEED89

PROD V=8,L=9,W=7ISO TEMP=110,PRES= 5.3END

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 R3.3TYPICAL SHORTCUT TRAYS

Column Section Minimum Trays

Naphtha - Kerosene

Kerosene - Diesel

Diesel - Gas oil

Gas oil -Topped crude

3.5 - 5.0

2.5 - 3.5

2.0 - 3.0

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.

Page 6: Crude Oil Distillation

SHORTCUT COLUMN OUTPUT

UNIT 1, ’SC01’, ’CRUDE TOWER’

FEEDS

STREAM PHASE------------ ------------1 MIXED WATR VAPOR

PRODUCTS

STREAM PHASE -------------------- MATERIAL BALANCES --------------------SECTION NO OF LB-MOL/HR LB/HR BBL/HRTRAYS

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

89 MIXED 2878.68 279901.38 1090.22 1 4.49WATER 1105.36 19913.15 56.89

10 LIQUID 1047.10 184786.42 641.70 2 3.7311 LIQUID 574.76 144886.42 477.04 3 2.7612 LIQUID 715.23 236618.47 747.78 4 1.4320 LIQUID 1337.39 695517.88 2043.50

TOTALS 7658.53 1561623.7 5057.14 12.41

SPECIFICATIONS

PARAMETER COMP. SPECIFICATION SPECIFIED CALCULATED TYPE NO TYPE VALUE VALUE----------------- ------------- ------------------------- -------------------- --------------------

STRM 89 D86 95 PCT 3.400E+02 3.400E+02STRM 10 D86 5 PCT 4.000E+01 4.000E+01STRM 10 D86 95 PCT 5.200E+02 5.200E+02STRM 11 D86 5 PCT 1.000E+01 9.999E+00STRM 11 D86 95 PCT 6.650E+02 6.650E+02STRM 12 D86 5 PCT -3.000E+01 -3.001E+01STRM 12 TBP 95 PCT 8.850E+02 8.850E+02STRM 20 TBP 5 PCT 6.950E+02 6.950E+02

Page 7: Crude Oil Distillation

SimulationModel(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

Page 8: Crude Oil Distillation

Input Data(Rigorous)

Virtually all the heat in the distillation enters with the crude oil feed, and so it is vitalthat 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 deter- mined in the shortcut simulation as initial estimates. The REFINERY model is usedto 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.

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 simultane- ously with the main column.

The column feed temperature is not calculated until after the column has been converged

Page 9: Crude Oil Distillation

Input Data File:

TITLE PROBLEM=R3R,PROJECT=APPBRIEFS,USER=SIMSCI,DATE=SEPT 90DIMEN PRES=PSIG,LIQV=BBL PRINT STREAM=SUMMARY,TBP COMPONENT DATALIBID 1,H2O/2,C2/3,C3/4,IC4/5,NC4/6,IC5/7,NC5THERMODYNAMIC DATAMETHODS SYSTEM=GS,COND=PETR,VISC(V)=PETR,VISC(L)=API STREAM DATAPROP STREAM=1,TEMP=450,PRES=14,PHASE=L,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

API STREAM=1,AVG=29.2LIGHT STREAM=1,PERCENT(V)=3,& COMP(V)=2,0.1/3,0.2/4,0.3/5,0.7/6,0.5/7,1.2PROP STREAM=2,TEMP=600,PRES=60,PHASE=V,RATE(W)=10000,& COMP=1,100PROP STREAM=3,TEMP=600,PRES=60,PHASE=V,RATE(W)=1500,& COMP=1,100PROP STREAM=4,TEMP=600,PRES=60,PHASE=V,RATE(W)=4500,& COMP=1,100PROP STREAM=5,TEMP=600,PRES=60,PHASE=V,RATE(W)=4000,& COMP=1,100NAME 1,CRUDE FEED/9,NAPHTHA/10,KEROSENE/11,DIESEL/&12,GAS OIL/20,TOPPED CRUDE UNIT OPERATIONSCOLUMN UID=COL1,NAME=CRUDE TOWER PARAM TRAY=20,DAMP=0.8

FEED 1,18/ 2,20/ 18,15/ 16,11/ 14,7COND TYPE=TFIX,TEMP=110PROD OVHD=9,2879,WATER=7,1,1105,BTMS=20,& LDRAW=15,8,1047/17,12,575/19,16,715DUTY 1,1/2,18/3,13,-40/4,9,-50/5,2,-50VARY DUTY=1,2PA FROM=14,TO=13,PHASE=L,TEMP=450PA FROM=10,TO=9,PHASE=L,TEMP=310PA FROM=3,TO=2,PHASE=L,TEMP=175PRESS 1,5.3/2,8.5/18,12.5/20,13.0ESTI MODEL=REFINERYSPEC COLUMN=COL1,TRAY=17,PHASE=L,RATE(V),RATIO,& STREAM=1,VALUE=0.03SPEC STREAM=9,D86(95),VALUE=340SIDESTRIPPER UID=SS01,NAME=KERO STRIP PARAM TRAY=2FEED 15,1/ 5,2

PROD OVHD=14,BTMS=10,1047PSPEC TOP=11.8SPEC STREAM=10,D86(95),VALUE=520

VARY FEED=15SIDESTRIPPER UID=SS02,NAME=DIESEL STRIP PARAM TRAY=2FEED 17,1/ 4,2PROD OVHD=16,BTMS=11,575PSPEC TOP=12.5SPEC STREAM=11,D86(95),VALUE=665VARY FEED=17SIDESTRIPPER UID=SS03,NAME=AGO STRIP PARAM TRAY=2FEED 19,1/ 3,2PROD OVHD=18, BTMS=12,715PSPEC TOP=13.3SPEC STREAM=12,TBP(95),VALUE=885VARY FEED=19FLASH UID=FL1,NAME=FEED TEMP FEED 1PROD M=1ADEFINE PRES AS COLUMN=COL1,TRAY=18,PRES DEFINE DUTY AS COLUMN=COL1,DUTY(2)END

Page 10: Crude Oil Distillation

COMPARISON OF SHORTCUT AND RIGOROUS RESULTS

The product qualities are compared below:

ASTM D86 (F)

LV%

Naphtha Kerosene Diesel Gas Oil

S/C Rig S/C Rig S/C Rig S/C Rig

05

10509095100

-5278130218314340376

-5278130218315340367

358380389433500520559

304374390431499520562

510530537585646665700

450513528585648665696

596635646715816842890

490613639717817842884

Bbl/hr

API

1090

61.5

1083

61.5

642

40.6

612

40.7

477

31.6

525

31.8

798

25.1

699

25.2

TBP @ 760 mm Hg (F)

LV%

Gas Oil Topped Crude

S/C Rig S/C Rig

05

10509095100

520611637727850885949

422593630728851885942

463695747972144715231548

548695743968144515221548

Bbl/hr

API

748

25.1

699

25.2

2043

14.1

2071

14.1

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.

Page 11: Crude Oil Distillation

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 FLASHFLASH ID FL1NAME FEED TEMP

FEEDS 1

PRODUCTS MIXED 1A

TEMPERATURE, F 695.117PRESSURE, PSIG 12.500PRESSURE DROP, PSI 1.500MOLE FRAC VAPOR 0.77043MOLE FRAC TOTAL LIQUID 0.22957MOLE FRAC H/C LIQUID 0.22957MOLE FRAC FREE WATER 0.00000DUTY, MM BTU/HR 291.79562FLASH TYPE ADIABATIC-P

Page 12: Crude Oil Distillation

CRUDE COLUMN SUMMARY

UNIT 1, ’COL1’, ’CRUDE TOWER’ TOTAL NUMBER OF ITERATIONS

IN/OUT METHOD 14

COLUMN SUMMARY

-------------------- NET FLOW RATES --------------------- HEATER TRAY TEMP PRESSURELIQUID VAPOR FEED PRODUCT DUTIES

DEG F PSIG LB-MOL/HR MM BTU/HR------------ ------------- ---------------- ---------------- ---------------- ----------------- ----------------- ------------------------1 110.0 5.30 2424.1 2875.9L -135.21941077.6W2 274.3 8.50 9778.5 6377.6 -50.00003 311.4 8.75 5091.8 8713.74 339.1 9.00 5017.3 9045.35 355.3 9.25 4849.2 8970.86 368.6 9.50 4573.5 8802.67 383.7 9.75 4122.9 8527.0 457.8V8 406.1 10.00 2284.7 7618.6 1248.2L9 438.6 10.25 6078.8 7028.5 -50.000010 471.1 10.50 3374.3 8300.211 503.9 10.75 2947.3 8118.1 437.2V12 533.0 11.00 1664.0 7254.0 829.4L13 562.7 11.25 3871.8 6800.0 -40.000014 592.8 11.50 2170.2 7455.415 619.5 11.75 1806.0 7306.2 164.9V16 642.8 12.00 486.2 6777.1 771.5L17 673.5 12.25 132.6 6228.818 693.5 12.50 1598.0 5875.2 6548.3M 291.795619 690.2 12.75 1477.6 792.320 684.4 13.00 671.8 555.1V 1360.9L

SIDESTRIPPER SS01

1/ 21 392.0 11.80 1139.5 1248.2L 457.8V

2/ 22 377.0 11.80 349.1 222.0V 1012.4L

SIDESTRIPPER SS02

1/ 23 519.5 12.50 740.8 829.4L 437.2V2/ 24 503.9 12.50 348.6 249.8V 642.0L

SIDESTRIPPER SS03

1/ 25 639.4 13.30 736.8 771.5L 164.9V2/ 26 633.3 13.30 130.2 83.3V 689.8L

Page 13: Crude Oil Distillation

CRUDE COLUMN SUMMARY (Cont)UNIT 1, ’COL1’, ’CRUDE TOWER’ (CONT) FEED AND PRODUCT STREAMS

TYPE STREAM PHASE FROM TO LIQUID FLOW RATES HEAT RATESTRAY TRAY FRACTION LB-MOL/HR MM BTU/HR

------------- ------------ ------------ -------- -------- ---------------- ------------------------ ------------------------FEED 14 VAPOR 7 0.0000 457.82 14.5426FEED 16 VAPOR 11 0.0000 437.20 18.6622FEED 18 VAPOR 15 0.0000 164.95 9.8699FEED 1 MIXED 18 0.5778 6548.34 326.2005FEED 2 VAPOR 20 0.0000 555.09 13.3040PRODUCT 9 LIQUID 1 2875.90 3.4362PRODUCT 7 WATER 1 1077.59 1.5132PRODUCT 15 LIQUID 8 1248.19 35.8340PRODUCT 17 LIQUID 12 829.36 49.0964PRODUCT 19 LIQUID 16 771.50 78.1636PRODUCT 20 LIQUID 20 1360.87 231.1219

SIDESTRIPPER SS01

FEED 15 LIQUID 21 1.0000 1248.19 35.8340FEED 5 VAPOR 22 0.0000 222.04 5.3216PRODUCT 14 VAPOR 21 457.82 14.5426PRODUCT 10 LIQUID 22 1012.40 26.6130

SIDESTRIPPER SS02

FEED 17 LIQUID 23 1.0000 829.36 49.0964FEED 4 VAPOR 24 0.0000 249.79 5.9868PRODUCT 16 VAPOR 23 437.20 18.6622PRODUCT 11 LIQUID 24 641.96 36.4206

SIDESTRIPPER SS03

FEED 19 LIQUID 25 1.0000 771.50 78.1636FEED 3 VAPOR 26 0.0000 83.26 1.9956PRODUCT 18 VAPOR 25 164.95 9.8699PRODUCT 12 LIQUID 26 689.81 70.2886

OVERALL MASS BALANCE, (FEEDS - PRODUCTS) 1.8405E-03OVERALL HEAT BALANCE, (H(IN) - H(OUT) ) -8.6010E-03

PUMPAROUNDS

TRAY TEMP, DEG F LIQUID FRACTION ------------------------ RATES -------------------------FROM TO FROM TO FROM TO LB-MOL/HR M LB/HR STD BBL/HR-------- -------- ------------- ------------- ------------- ------------- -------------------- -------------------- --------------------

14 13 592.8 450.0 1.0000 1.0000 1552.37 422.898 1374.4510 9 471.1 310.0 1.0000 1.0000 2522.48 505.309 1719.863 2 311.4 175.0 1.0000 1.0000 5018.31 654.301 2385.77

Page 14: Crude Oil Distillation

UNIT 1, ’COL1’, ’CRUDE TOWER’ (CONT) SPECIFICATIONS

PARAMETER TRAY COMP SPECIFICATION SPECIFIED CALCULATED TYPE NO NO TYPE VALUE VALUE----------------- -------- ------------ ------------------------- -------------------- --------------------TRAY LIQ 17 VOL RATIO 3.000E-02 3.002E-02

STRM 9 1 D86 95 PCT 3.400E+02 3.400E+02STRM 10 22 D86 95 PCT 5.200E+02 5.200E+02STRM 11 24 D86 95 PCT 6.650E+02 6.651E+02STRM 12 26 TBP 95 PCT 8.850E+02 8.851E+02

PRODUCT STREAM SUMMARYSTREAM ID 10 11 12 14NAME KEROSENE DIESEL GAS OILPHASE WET LIQUID WET LIQUID WET LIQUID WET VAPOR

--------- TOTAL STREAM ---------RATE, LB-MOL/HR 1012.402 641.956 689.814 457.823M LB/HR 175.903 158.610 224.796 39.007

TEMPERATURE, F 377.003 503.923 633.265 391.983PRESSURE, PSIG 11.800 12.500 13.300 11.800MOLECULAR WEIGHT 173.748 247.073 325.880 85.202ENTHALPY, MM BTU/HR 26.613 36.421 70.289 14.543

BTU/LB 151.294 229.623 312.677 372.817MOLE FRACTION LIQUID 1.00000 1.00000 1.00000 0.00000MOLE FRACTION FREE WATER 0.00000 0.00000 0.00000 0.00000

--------- TOTAL VAPOR ------------RATE, LB-MOL/HR N/A N/A N/A 457.823M LB/HR N/A N/A N/A 39.007M FT3/HR N/A N/A N/A 154.537STD VAP RATE(1), M FT3/HR N/A N/A N/A 173.735MOLECULAR WEIGHT N/A N/A N/A 85.202ENTHALPY, BTU/LB N/A N/A N/A 372.817

CP, BTU/LB-F N/A N/A N/A 0.537DENSITY, LB/M FT3 N/A N/A N/A 252.414THERMAL COND, BTU/HR-FT-F N/A N/A N/A 0.01652

VISCOSITY, CP N/A N/A N/A 0.01088

--------- TOTAL LIQUID ---------RATE, LB-MOL/HR 1012.402 641.956 689.814 N/A

M LB/HR 175.903 158.610 224.796 N/ABBL/HR 724.057 645.271 917.344 N/AGAL/MIN 506.838 451.688 642.139 N/A

STD LIQ RATE, BBL/HR 611.476 523.015 711.077 N/AMOLECULAR WEIGHT 173.748 247.073 325.880 N/AENTHALPY, BTU/LB 151.294 229.623 312.677 N/ACP, BTU/LB-F 0.614 0.657 0.707 N/ADENSITY, LB/BBL 242.941 245.804 245.051 N/ATH COND, BTU/HR-FT-F 0.05023 0.04356 0.03833 N/AVISCOSITY, CP 0.27647 0.27529 0.27323 N/A

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

Page 15: Crude Oil Distillation

PRES (KAYS RULE) 0.0807 0.1096 0.1439 0.0704

PRODUCT STREAM SUMMARY (Cont)

STREAM ID 10 11 12 14NAME KEROSENE DIESEL GAS OILPHASE WET LIQUID WET LIQUID WET LIQUID WET VAPOR

------------ DRY STREAM ------------RATE, LB-MOL/HR 1004.161 636.901 685.516 242.392M LB/HR 175.754 158.519 224.719 35.126

STD LIQ RATE, BBL/HR 611.052 522.755 710.856 125.822MOLECULAR WEIGHT 175.026 248.891 327.810 144.916MOLE FRACTION LIQUID 1.0000 1.0000 1.0000 0.0000REDUCED TEMP (KAYS RULE) 0.6824 0.7001 0.7293 0.7465

ACENTRIC FACTOR 0.5145 0.6311 0.7448 0.4487WATSON K (UOPK) 11.733 11.732 11.732 11.744STD LIQ DENSITY, LB/BBL 287.626 303.238 316.124 279.177

SPECIFIC GRAVITY 0.8214 0.8660 0.9028 0.7973API GRAVITY 40.765 31.896 25.235 45.978

------------ DRY VAPOR -------------RATE, LB-MOL/HR N/A N/A N/A 242.392

M LB/HR N/A N/A N/A 35.126M FT3/HR N/A N/A N/A 80.545

STD VAP RATE(1), M FT3/HR N/A N/A N/A 91.983SPECIFIC GRAVITY (AIR=1.0) N/A N/A N/A 5.003MOLECULAR WEIGHT N/A N/A N/A 144.916Z (FROM K) N/A N/A N/A 0.9695CP, BTU/LB-F N/A N/A N/A 0.544DENSITY, LB/M FT3 N/A N/A N/A 436.106THERMAL COND, BTU/HR-FT-F N/A N/A N/A 0.01532VISCOSITY, CP N/A N/A N/A 0.00920

------------ DRY LIQUID ------------RATE, LB-MOL/HR 1004.161 636.901 685.516 N/A

M LB/HR 175.754 158.519 224.719 N/ABBL/HR 723.572 644.938 916.993 N/AGAL/MIN 506.499 451.455 641.893 N/A

STD LIQ RATE, BBL/HR 611.052 522.755 710.856 N/ASPECIFIC GRAVITY (H2O=1.0) 0.8214 0.8660 0.9028 N/AMOLECULAR WEIGHT 175.026 248.891 327.810 N/AZ (FROM K) 0.0000 0.0000 0.0000 N/ACP, BTU/LB-F 0.614 0.657 0.707 N/ADENSITY, LB/BBL 242.898 245.790 245.061 N/ATHERMAL COND, BTU/HR-FT-F 0.05020 0.04355 0.03832 N/AVISCOSITY, CP 0.27786 0.27714 0.27494 N/A

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

Page 16: Crude Oil Distillation

0 LV PERCENT -5.793 -5.793 -82.191 242.064

0 LV PERCENT -136.159 -136.159 -192.547 52.528

PRODUCT DISTILLATION CURVESSTREAM ID 1 1A 9 10NAME CRUDE FEED NAPHTHA KEROSENE

TBP AT 760 MM HG

5 147.566 147.566 42.967 340.41210 208.225 208.225 93.091 360.88030 459.057 459.057 171.290 401.00750 689.818 689.818 217.790 434.65870 864.505 864.505 269.335 471.15190 1240.591 1240.591 331.246 520.62895 1414.367 1414.367 352.148 542.111100 1547.776 1547.776 375.169 583.764

TBP AT 10 MM HG

5 -20.472 -20.472 -99.743 129.93610 26.235 26.235 -61.953 146.23430 225.327 225.327 -2.270 178.37650 417.429 417.429 33.649 205.52770 568.937 568.937 73.844 235.17690 914.411 914.411 122.659 275.71895 1083.646 1083.646 139.273 293.447100 1218.001 1218.001 157.650 328.038ASTM D86

0 LV PERCENT 29.766 29.766 -52.478 296.4275 181.851 181.851 77.957 372.10410 242.008 242.008 130.195 387.85430 465.239 465.239 185.348 409.10950 679.107 679.107 217.630 430.17270 834.151 834.151 262.078 456.92390 1192.319 1192.319 315.191 498.49795 1334.165 1334.165 340.009 520.046100 1443.061 1443.061 367.342 561.824

ASTM D11600 LV PERCENT -22.476 -22.476 -41.402 297.840

5 140.822 140.822 67.857 361.44310 205.329 205.329 111.705 374.73530 457.986 457.986 179.475 407.47650 689.818 689.818 217.790 434.65870 864.505 864.505 269.335 471.15190 1240.591 1240.591 331.246 520.62895 1414.367 1414.367 352.148 542.111100 1547.776 1547.776 375.169 583.764

ASTM D86 WITH CRACKING0 LV PERCENT 29.766 29.766 -52.478 296.427

5 181.851 181.851 77.957 372.10410 242.008 242.008 130.195 387.85430 465.239 465.239 185.348 409.10950 648.793 648.793 217.630 430.17270 746.392 746.392 262.078 456.92390 866.448 866.448 315.191 492.94395 895.100 895.100 340.009 513.127100 918.582 918.582 367.342 551.333

Page 17: Crude Oil Distillation