Two stage hydrocracking of vacuum gas oil

(1)

augustus 1993

,J~fi

T

U

Delft

Technische Universiteit Delft

TWO STAGE HYDROCRACKING

of vacuum gas oil

ASPEN modellering

behorende bij FVO no. 3012.

Johan Hoorn

Robert Stockmann

(2)

AS PEN PLUS input

output en subroutines

ASPEN PLUS RELEASE 8 BIJLAGE

Hier volgen achtereenvolgens

crack3.inp

crack3.rep .

heatex.inp

heatex.rep .

hdscra.f

yldusr.f

BIJLAGE 4

crack3

is de RUN identifier van de TWO STAGE HYDROCRACKER. Deze run bevat

het flowsheet van de hydrocracker (zie het flowsheet-shema). crack3.inp is

de inputfile en crack3.rep de outputfile.

heatex is de RUN identifier van de warmtewisselaar simulatie.

hdscra.f is de subroutine voor een reactorbed van de lst stage reaktor.

Het reactormodel is geimplementeerd in de optie SUBROUTINE van het aspen

reactor model RYIELD. Reactor R6 heeft 3 bedden, in aspen voeren we dit

in door 3 blokken RYIELD te definieren, R6A R6B en R6C.

Inputparameters in de inputfile zijn resp. A, B, tijd en conv. conv is

conversie van de HDS en HDN reactie.

yldusr.f is de subroutine voor een reactorbed van de 2nd stage reaktor.

Inputparameters in de inpufile zijn resp. A, B en tijd. Reactor

R7 is opgedeeld in 5 bedden. In aspen zijn dit dan weer 5 blokken RYIELD

te weten R7A

tlm

R7E. Tussen de reactor bedden van R6 en R7 worden waterstof

quench stromen toegevoerd. Door met de grootte van de quench stromen en de

parameter tijd (evenredig met de bedlengte) te spelen, kunnen we de

adiabatische temperatuur stijging per bed met aspen simuleren.

De beide subroutines moeten gecompileerd worden op de dutsh12, of dutsh5

volgens:

f77 -c +ppu -w -K +El +T +DAl.O +800 hdscra.f

de resulterende objectfiles (hdscra.o) worden dan met de aspen

executable meegelinkt.

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-HYDROGEN DIVl4 R 6 R 7 T 12 T 17 T 23 T 26 T 27 12. ~ 1J4' IU MlO CB DIVl3 1I10A M7

"

,.

DIVlI f-<ID--M--PC

IST STAGE REACTOR: DESULtifliZATION. DENITRltiCATION AND MILD HYDROCRACKING

2ND STAGE REACTOR: MAIN HYDROCRACKING

PACKED A13S0RPTION COLUMN rOR H2S REMOVAL STEAM STRIPPING COLUMN rOR H2S REMOVAL MAIN rRACTIONA TOR

KEROSINE SI DE STRIPPING COLUMN DIESEL SIDE STRIPPING COLUMN

DIVl2 -)8" purge P21 H2S/GAS

..

.)() Ko .• T23 L-.®--~ LIGHT NAPHTA '--<E>-~ WATER ---<E>-MP STEAM -!>]"}01IJQ GAS WATER NAPHTA T26 MP STEAM --®-_~ T27 KEROSINE DIESEL

TWO STAGE HYDROCRACKING OF VACUUM GAS Oll J.A.A. Hoorn ond R.M. Slockmonn fabrieksvoorontwerp No. J012 August 1993

(4)

iInput file created by ModelManager Rel. 3

.

3-4 on Thu Aug 12 23:47:38 1993

iDirectory

/horne/dutsh5/aio/stock

Runid CRACK3

TITLE "Two stage Hydrocracker"

IN-UNITS SI

DEF-STREAMS CONVEN ALL

SIM-OPTIONS RESTART=YES

SYS-OPTIONS OEBUG=YES

ACCOUNT-INFO ACCOUNT=ONBRKI3 PROJECT-IO=CRACK

&

PROJECT-NAME="KRAAK

MÀÀR

RAAK" USER-NAME="STOCK ANO HOORN"

RUN-CONTROL MAX-TIME=300

OESCRIPTION "This run sirnulates a hydrocracker.

For the first stage reactor, the user defined

subroutine hdscra.f is used and the second

stage reactor uses yldusr.f as subroutine. "

PC-USER

PC-OEF API-METH Fl NBP=525 <C> LOEN=980 MW=480

PC-OEF API-METH F2 NBP=475

<C>

LOEN=950 MW=430

PC-OEF API-METH F3 NBP=425

<C>

LOEN=920 MW=375

PC-OEF API-METH F4 NBP=375

<C>

LOEN=890 MW=325

PC-OEF API-METH F5 NBP=325 <C> LOEN=860 MW=275

PC-OEF API-METH F6 NBP=275 <C> LOEN=835 MW=225

PC-OEF API-METH F7 NBP=225 <C> LOEN=810 MW=185

PC-OEF API-METH F8 NBP=175

<C>

LOEN=785 MW=145

PC-OEF API-METH F9 NBP=125

<C>

LOEN=760 MW=115

PC-OEF API-METH FI0 NBP=75 <C> LOEN=735 MW=88

PC-OEF API-METH Fll NBP=25 <C> LOEN=710 MW=60

PC-OEF API-METH SSC NBP=425 <C> MW=320.64

PC-OEF API-METH NSC NBP=375 <C> MW=280.14

OATABANKS ASPENPCO

PROP-SOURCES ASPENPCO

COMPONENTS

Fl

*

Fl

_/

F2

*

F2

_/

F3

*

F3

_/

F4

*

F4

_/

F5

*

F5

_/

F6

*

F6

_/

F7

*

F7

_/

F8

*

F8

_/

F9

*

F9 /

(5)

NH3 H3N NH3 /

SSC

*

SSC /

NSC

*

NSC /

H20 H20 H20

FLOWSHEET

BLOCK MIXERI IN=9 7 OUT=8

BLOCK F4 IN=8 OUT=ll

BLOCK R6A IN=ll OUT=llA

BLOCK H9 IN=17 OUT=25

BLOCK V13 IN=25 OUT=28 31

BLOCK V14 IN=31 OUT=35 36

BLOCK Hll

IN=36

OUT=40

BLOCK T17 IN=40 45 OUT=41 42

BLOCK MIXER2 IN=10 3 OUT=5

BLOCK F5 IN=5 OUT=12

BLOCK R7A IN=12 OUT=12A

BLOCK H15 IN=33 OUT=32

BLOCK V16 IN=32 OUT=37 39

BLOCK V18 IN=39 OUT=43 44

BLOCK MIXER3 IN=42 44 OUT=47

BLOCK F22 IN=48 OUT=52

BLOCK P21 IN=53 OUT=10

BLOCK DIVl1 IN=27 OUT=8B 29

BLOCK Cl IN=l OUT=lA

BLOCK T12 IN=28 OUT=27 30

BLOCK DIVI2 IN=37 OUT=38 34

BLOCK C8 IN=26 OUT=22

BLOCK MIXER7 IN=8B 34 OUT=26

BLOCK DIVI3 IN=16A OUT=18 19 20 21 15 16

BLOCK MIXER8 IN=12A 18 OUT=12B

BLOCK R7B IN=12B OUT=12C

BLOCK MIXER9 IN=12C 19 OUT=12D

BLOCK R7C IN=12D OUT=12E

BLOCK H19 IN=41 OUT=46

BLOCK V20 IN=46 OUT=49 50 51

BLOCK P2 IN=2 OUT=4

BLOCK MIXERIO IN=22 6 OUT=16A

BLOCK MIXERll IN=12E 20 OUT=12F

BLOCK R7D IN=12F OUT=12G

BLOCK MIXER12 IN=12G 21 OUT=12H

BLOCK R7E IN=12H OUT=14

BLOCK MIXER13 IN=llA 15 OUT=llB

BLOCK R6B IN=llB OUT=llC

BLOCK MIXER14 IN=llC 16 OUT=llD

BLOCK R6C IN=llD OUT=13

BLOCK MULFRAC IN=52 59 54 OUT=56 55 53 60 58 57

BLOCK COOL5 IN=55 OUT=NAPHTA

BLOCK COOL6 IN=60 OUT=KERO

BLOCK COOL7 IN=58 OUT=DIESEL

BLOCK DIVI4 IN=lA OUT=7 3 6

BLOCK H3A IN=4 OUT=9

BLOCK H3 IN=13 OUT=17

BLOCK HIOA IN=14 OUT=24

BLOCK HIO IN=47 OUT=48

BLOCK HIlA IN=24 OUT=33

BLOCK SEPN IN=NAPHTA OUT=WATERN NA

BLOCK SEPK IN=KERO OUT=WATERK KE

BLOCK SEPD IN=DIESEL OUT=WATERD DI

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PROPERTIES SYSOP4

PROP-REPLACE SYSOP4 SYSOP4

PROP HLMX HLMXO 4

PROP VLMX VLMXOl

PROP-DATA HFORM

IN-UNITS SI

PROP-LIST DHFORM

PVAL Fl 0

PVAL F2 0

PVAL F3 0

PVAL F4 0

PVAL F5 0

PVAL F6 0

PVAL F7 0

PVAL F8 0

PVAL F9 0

PVAL FIO 0

PVAL Fll 0

PVAL H2S 0

PVAL NH3 0

PVAL SSC 0

PVAL NSC 0

PVAL H20 0

PROP-SET KONSTANT CETANENO REFINDEX ANILPT API VISINDEX WAT

&

TBPCRV UNITS='C' SUBSTREAM=MIXED

STREAM 1

SUBSTREAM MIXED TEMP=25 <C> PRES=40 <BAR>

MASS-FLOW H2 1.5

STREAM 16

SUBSTREAM MIXED TEMP=25 <C> PRES=40 <BAR>

MASS-FLOW H2 1.50

STREAM 16A

SUBSTREAM MIXED TEMP=320 PRES=120 <BAR>

MASS-FLOW H2 4.9

STREAM 2

SUBSTREAM MIXED TEMP=25 <C> PRES=l <BAR>

MASS-FLOW F1 3.753 / F2 13.7934 / F3 12.7211 / F4

&

10.9665 / F5 5.2152 / F6 2.2908 / SSC 1.2 / NSC

&

0.06 STREAM 44

SUBSTREAM MIXED TEMP=320 PRES=5.0E5

MASS-FLOW F1 0.38 / F2 1.82 / F3 2.91 / F4 5.22 /

&

F5 4.75 / F6 6.26 / F7 5.96 / F8 5.25 / F9 3.79

&

/ F10 1.94 / Fll 0.39

STREAM 45

SUBSTREAM MIXED TEMP=220 <C> PRES=10

<BAR>

(7)

11.6334 / F5 2.3634 / F6 0.9586 / F7 0.3164 / F8

&

9.5790E-2 / F9 1.6561E-2 / FI0 1.2745E-3 / Fll

&

4.0722E-5 / H20 5.3167E-5

STREAM 54

SUBSTREAM MIXED TEMP=220

<C>

PRES=10 <BAR>

MASS-FLOW H20 2

STREAM 59

SUBSTREAM MIXED TEMP=220

<C>

PRES=10 <BAR>

MASS-FLOW H20 2

BLOCK MIXERI MIXER

BLOCK MIXERI0 MIXER

BLOCK MIXERll MIXER

BLOCK MIXER12 MIXER

BLOCK MIXER13 MIXER

BLOCK MIXER14 MIXER

BLOCK MIXER2 MIXER

BLOCK MIXER3 MIXER

BLOCK MIXER7 MIXER

BLOCK MIXER8 MIXER

BLOCK MIXER9 MIXER

BLOCK DIVII FSPLIT

FRAC 29 0.05

BLOCK DIVI2 FSPLIT

MASS-FLOW 34 2.5

BLOCK DIVI3 FSPLIT

MASS-FLOW 19 0.66 / 20 0.66 / 21 0.66 / 15 0.5 / 16

&

0.5 BLOCK DIVI4 FSPLIT

MASS-FLOW 7 0.5 / 3 0.7

BLOCK SEPD SEP

FRAC STREAM=WATERD SUBSTREAM=MIXED COMPS=Fl F2 F3 F4 F5

&

F6 F7 F8 F9 FI0 Fll H2 H2S NH3 SSC NSC H20 FRACS=

&

o

0 0 0 0 0 0 0 0 0 0 1 1 1 1 1 1

BLOCK SEPK SEP

FRAC STREAM=KE SUBSTREAM=MIXED COMPS=Fl F2 F3 F4 F5 F6

&

F7 F8 F9 FI0 Fll H2 H2S NH3 SSC NSC H20 FRACS=l

&

1 1 1 1 1 1 1 1 1 1 0 0 0 0 0 0

BLOCK SEPN SEP

FRAC STREAM=NA SUBSTREAM=MIXED COMPS=Fl F2 F3 F4 F5 F6

&

(8)

1 1 1 1 1 1 1 1 1 1 0 0 0 0 0 0

BLOCK T12 SEP

FRAC STREAM=27 SUBSTREAM=MIXED COMPS=F1 F2 F3 F4 F5 F6

&

F7 F8 F9 F10 F11 H2 H2S NH3 SSC NSC H20 FRACS=l

&

1 1 1 1 1 1 1 1 1 1 1 .10 .10 1 1 1

BLOCK COOL5 HEAT ER

PARAM TEMP=25 <C> PRES=l <BAR>

BLOCK COOL6 HEATER

PARAM TEMP=25 <C> PRES=l <BAR>

BLOCK COOL7 HEATER

PARAM TEMP=25 <C> PRES=l <BAR>

BLOCK F22 HEATER

PARAM TEMP=330 <C> PRES=5 <BAR>

BLOCK F4 HEATER

PARAM TEMP=385 <C> PRES=119 <BAR>

BLOCK F5 HEATER

PARAM TEMP=380 <C> PRES=119 <BAR>

BLOCK H10 HEATER

PARAM TEMP=270 <C> PRES=4 <BAR>

BLOCK HIOA HEAT ER

PARAM TEMP=150 <C> PRES=113.8 <BAR>

BLOCK H11 HEAT ER

PARAM TEMP=120 <C> PRES=5 <BAR>

BLOCK HIlA HEATER

PARAM TEMP=90 <C> PRES=113.5 <BAR>

BLOCK H15 HEAT ER

PARAM TEMP=40 <C> PRES=113 <BAR>

BLOCK Hl9 HEATER

PARAM TEMP=30 <C> PRES=5 <BAR>

BLOCK H3 HEATER

PARAM TEMP=177 <C> PRES=113.5 <BAR>

BLOCK H3A HEAT ER

PARAM TEMP=350 <C> PRES=118.5 <BAR>

BLOCK H9 HEAT ER

PARAM TEMP=40 <C> PRES=113 <BAR>

BLOCK V13 FLASH2

PARAM PRES=113 <BAR> DUTY=Q

BLOCK V14 FLASH2

(9)

BLOCK V18 FLASH2

PARAM PRES=5.5 <BAR> DUTY=O

BLOCK V20 FLASH3

PARAM TEMP=30

<C>

PRES=l <BAR>

PROPERTIES SYSOP4

BLOCK MULFRAC MULTIFRAC

PARAM NCOL=3 NSTAGE=22 NIC-STREAM=4 ALGORITHM=SUM-RATES

&

INIT-OPTION=CRUDE

FEEDS 52 1 15 ON-STAGE

/ 59 2 2 ON-STAGE

/ 54

&

3 2 ON-STAGE

PRODUCTS 55 1 1 PHASE=L / 56 1 1 PHASE=V / 53 1 18

&

PHASE=L / 60 2 2 PHASE=L / 58 3 2 PHASE=L / 57

&

1 1 PHASE=W

P-SPEC 1 1 1 <BAR>

P-SPEC 2 1 1 <BAR>

P-SPEC 3 1 1 <BAR>

COL-SPECS 1 NSTAGE=18 MASS-B=38 QN=2.5E8 MASS-RDV=0.02

COL-SPECS 2 NSTAGE=2 Q1=0 QN=O

COL-SPECS 3 NSTAGE=2 Q1=0 QN=O

CONNECT-STRE 1 SOURCE-COL=l 10 DEST-COL=3 1 MASS-FLOW=20

CONNECT-STRE 2 SOURCE-COL=3 1 DEST-COL=l 9 PHASE=V

CONNECT-STRE 3 SOURCE-COL=l 5 DEST-COL=2 1 MASS-FLOW=15

CONNECT-STRE 4 SOURCE-COL=2 1 DEST-COL=l 4 PHASE=V

T-EST 1 1 85

<C> /

1 18 400

<C>

T-EST 2 1 175

<C> /

2 2 180

<C>

T-EST 3 1 275

<C> /

3 2 280

<C>

VARY 1 IC-MASS-FLOW 0 50 IC-STREAM=3

VARY 2 IC-MASS-FLOW 0 50 IC-STREAM=l

VARY 3 QN 10000 1E10 COL=l

SPEC 1 MASS-FLOW 16 COL=2 STAGE=2

SPEC 2 MASS-FLOW 25.5 COL=3 STAGE=2

SPEC 3 MASS-FLOW 38 COL=l STAGE=18

PLOT 2 VRATE BASIS=MASS PRINT-PLOT=NO PLOT-FILE=YES

PLOT 1 LRATE BASIS=MASS PRINT-PLOT=NO PLOT-FILE=YES

PROPERTIES SYSOP4

BLOCK-OPTION FREE-WATER=YES

BLOCK T17 ABSBR

PARAM NSTAGE=10

FEEDS 40 10 / 45 1

PRODUCTS 41 10 / 42 1

P-SPEC 10 5 <BAR> / 1 5.5 <BAR>

BLOCK R6A RYIELD

SUBROUTINE YIELD=HDSCRA

USER-VECS NREAL=4

REAL VALUE-LIST=0.5 -0.5 0.1 0.33

PARAM PRES=117.2 <BAR> DUTY=O

BLOCK R6B RYIELD

SUBROUTINE YIELD=HDSCRA

USER-VECS NREAL=4

REAL VALUE-LIST=0.5 -0.5 0.1 0.5

PARAM PRES=116.3 <BAR> DUTY=O

BLOCK R6C RYIELD

(10)

USER-VECS NREAL=4

REAL VALUE-LIST=0.5 -0.5 0.1 1

PARAM PRES=115.3 <BAR> DUTY=O

BLOCK R7A RYIELD

SUBROUTINE YIELD=YLDUSR

USER-VECS NREAL=3

REAL VALUE-LIST=0.5 -0.5 0.1

PARAM PRES=118.2 <BAR> DUTY=O

BLOCK R7B RYIELD

SUBROUTINE YIELD=YLDUSR

USER-VECS NREAL=3

REAL VALUE-LIST=0.5 -0.5 0.15

PARAM PRES=117.7 <BAR> DUTY=O

BLOCK R7C RYIELD

SUBROUTINE YIELD=YLDUSR

USER-VECS NREAL=3

REAL VALUE-LIST=0.5 -0.5 0.2

PARAM PRES=117 <BAR> DUTY=O

BLOCK R7D RYIELD

SUBROUTINE YIELD=YLDUSR

USER-VECS NREAL=3

REAL VALUE-LIST=0.5 -0.5 0.25

PARAM PRES=116.1 <BAR> DUTY=O

BLOCK R7E RYIELD

SUBROUTINE YIELD=YLDUSR

USER-VECS NREAL=3

REAL VALUE-LIST=0.5 -0.5 0.3

PARAM PRES=115 <BAR> DUTY=O

BLOCK P2 PUMP

PARAM PRES=120 <BAR>

BLOCK P21 PUMP

PARAM PRES=120 <BAR>

BLOCK Cl COMPR

PARAM TYPE=ISENTROPIC PRES=120 <BAR>

BLOCK C8 COMPR

PARAM TYPE=ISENTROPIC PRES=120 <BAR>

CONV-OPTIONS

TEAR

PARAM TEAR-METHOD=WEGSTEIN TOL=0.0005

WEGSTEIN MAXIT=50 QMIN=-10

TEAR 16A 0.0005 / 44 0.0005

STREAM-REPOR NOSORT NOMOLEFLOW MASSFLOW NOVOLFLOW NOMOLEFRAC

&

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CRACK3.REP 13/08/1993 + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + + + ... ... ... + + + + + + + + ... + ... + + + + + + + + + + + + + + + + + + + + +.+ + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ++ + + ++ + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + +++++++++ + + + + +++++++++ ++++++ ++ + + + + ++ ++++++ +++++ + + + + + + +++++ +++++ + + + + + + +++++ +++++ + + + + + + +++++ +++++ + + + + + + +++++ +++++ + + + ... + + +++++ + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + +++++++++ + + + + +++++++++ +++++++++ + + ... + +++++++++ + + + + + + + + +++++++++ + ... + ... +++++++++ + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + ... ... + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + + ... + + + + + + + + + + + + + + + + + + + + + + + + MAM A A AAAM A A A A SSSSS S SSSSS S SSSSS PPPPP P P PPPPP P P EEEEE E EEEEE E EEEEE ASPEN PLUS IS A TRADEMARK OF ASPEN TECHNOLOGY, INC.

251 VASSAR STREET CAMBRIDGE

Ó

MASSACHUSETTS 02139 617/497·9 10 VERSION: HP-PA RELEASE: 8.5-4 INSTALLATION: DUTSCH5 NN N N N N N N N N NN N N ppppp p P PPPPP P P HOTl! NE: L L L L LLLLL u U U U U U U U UUUUU U.S.A. 617/497-9010 EUROPE (32) 2/732-6300 AUGUST 13, 1993 FRIDAY 12:04:05 A.M. TM SSSSS S SSSSS S SSSSS

(12)

T~O STAGE HYDROCRACKER

ASPEN PLUS(TM) [S A PROPR[ETARY PRODUCT OF ASPEN TECHNOLOGY. [NC. (ASPENTECH). AND MAY BE US EO ONLY UNDER AGREEMENT ~[TH ASPENTECH.

RESTR[CTED R[GHTS LEGEND: USE. DUPL[CAT[ON. OR D[SCLOSURE BY THE

GOVERNMENT [S SUBJECT TO RESTR[CT[ONS AS SET FORTH [N DEAR AND DFAR 252-227-7013 (C)(1)([[) OF THE R[GHTS [N TECHN[CAL DATA AND COMPUTER

SOFT~ARE CLAUSES OR OTHER S[M[LAR REGULAT[ONS OF OTHER GOVERNMENTAL AGENC[ES ~H[CH DES[GNATE SOFT~ARE AND DOCUMENTAT[ON AS PROPR[ETARY.

TABLE OF CONTENTS

RUN CONTROL SE CT [ON ...•...

RUN CONTROL [NFORMAT[ON ...•••....• DESCR[PT[ON ...•...•...

BLOCK STATUS ...•...•...

FLO~SHEET SECT[ON... 2

FLO~SHEET CONNECTIVITY BY STREAMS ... 2

FLO~SHEET CONNECTIV[TY BY BLOCKS ... 2

CONVERGENCE STATUS SUMMARY .•..•...• 3

CONVERGENCE BLOCK: $OLVER01 •.•... 4

COMPUTAT IONAL SEQUENCE... 5

OVERALL FLO~SHEET BALANCE... 5

PHYSICAL PROPERTIES SECTION ...•••••.•.. 7

COMPONENTS. . . • . . . • . . . • . • . • . . • . . 7

U-O-S BLOCK SECTION .•••••...•••.••• 8

BLOCK: C1 MODEL COMPR... ... 8

BLOCK: C8 MODEL COMPR. . • . . . • . • • . . . 8

BLOCK: COOL5 MODEL HEATER ••.•... 9

BLOCK: COOL6 MODEL HEATER ••.•.•... 10

BLOCK: COOL7 MODEL HEATER ••••.•.•.... 11

BLOCK: DIVI1 MODEL FSPLIT •.••.•.••... 12

BLOCK: DIVI2 MODEL FSPLIT ...•... 13

BLOCK: DIVI3 MODEL FSPLIT ... 13

BLOCK: DIVI4 MODEL FSPLIT ...•••. 14

BLOCK: F22 MODEL HEATER. • • . • . . . .. 14

BLOCK: F4 MODEL HEATER ...••... 15

BLOCK: F5 MODEL HEA TER. . . . • • . • •. 16

BLOCK: H10 MODEL HEATER ...•..•. 17

BLOCK: H 1 OA MODEL HEATER.. . . .. 18

BLOCK: H11 MODEL HEATER ... 19

BLOCK: H 11 A MODEL HEATER. . . . • .. 20

BLOCK: H15 MODEL HEATER ...••..• 21

BLOCK: H3A MODEL HEATER ...•... 24

BLOCK: H9 MODEL HEATER •... 25

T~O STAGE HYDROCRACKER TABLE OF CDNTENTS BLOCK M[XER12 MODEL M[XER .•...•• 27

BLOCK M[XER13 MODEL M[XER ••.••....•... 28

BLOCK M[XER14 MODEL M[XER ...•.•. 28

BLOCK M[XER2 MODEL M[XER •••...•... 29

BLOCK M[XER3 MODEL M[XER .••..•...•• 29

BLOCK M[XER7 MODEL M[XER •••••....•.•. 30

BLOCK M[XER8 MODEL M[XER ... 30

BLOCK M[XER9 MODEL M[XER •... 30

BLOCK MULFRAC MODEL MULT[FRAC .•••••..• 31

BLOCK P2 MODEL PUMP ... 43

BLOCK P21 MODEL PUMP •.•... 44

BLOCK R6A MODEL RY[ELD ...•... 44

BLOCK R6B MODEL RYI ELD •.•.•... 46

BLOCK R6C MODEL RY[ELD ••...•.••• 48

BLOCK R7A MODEL RY[ELD •...•... 50

BLOCK R7B MODEL RY[ELD •....•... 52

BLOCK R7c MODEL RYI ELD ... 54

BLOCK R7D MODEL RY[ELD ... 56

BLOCK R7E MODEL RYI ELD .•..•... 58

BLOCK SEPD MODEL SEP •••.•... 60

BLOCK SEPK MODEL SEP ... 62

BLOCK SEPN MODEL SEP •.••••....•.... 65

BLOCK T12 MODEL SEP ...••.••• 67

BLOCK T17 MODEL ABSBR ...•... 69

BLOCK VU MODEL FLASH2 ••...•.••••• 72

BLOCK V14 MODEL FLASH2 •...•.•....• 73

BLOCK V16 MODEL FLASH2 .•..•..•.•.. 74

BLOCK V18 MODEL FLASH2 •....•.•.•.. 75

BLOCK V20 MODEL FLASH3 ... 76

STREAM SECT ION. • • . . . • . . • . • . . . .. 78

DESCRIPTION OF STREAM CLASS ••••...••.•.... 78

45 1 2 54 59... 79 8 11 11A 25 28 ...••...•.•....• 80 31 35 36 40 41. ...•..•...•..• 81 42 5 12 12A 32 .•....••.•... 82 3739 43 44 47 •••••.••••... 83 52 10 8B 29 1A .••...•...•.•• 84 2730 38 34 22 ...•....••....•...•.. 85 26 18 19 20 21. ..••.•••...•... 86 15 16 12B 12C 120 ....•...•• 87 12E 46 49 50 51 ..••..•...• 88 4 16A 12F 12G 12H ••.••.•... 89 14 11B 11C 110 13 ••..•••... 90 56 55 53 60 58 •...•... 91

57 NAPHTA KERO DIESEL 7 ....•...••• 92

3 6 9 17 24 ...•••...•... 93

48 33 ~ATERN NA ~ATERK •... 94

(13)

-

- -

I

RUN CONTROL INFORMATION

TYO STAGE HYDROCRACKER

RUN CONTROL SECTION

THIS VERSION OF ASPEN PLUS LICENSEO TO Delft University of Technology

THE FOLLO~ING LAYERED PROOUCTS HAVE BEEN INSTALLED:

RATEFRAC RELEASE 1.5-4 INSTALLED ON 07/21/92 AT 19:51:30:00

TYPE OF RUN: NE~

INPUT fILE NAME: crack3.inp

OUTPUT PROBLEM DATA fILE NAME: crack3 VERSION NO.

LOCATED IN: /home/dutsh5/aio/stock

POF SIZE USED fOR INPUT TRANSLATION:

NUMBER Of FILE RECORDS (PSIZE) 9999

NUMBER Of IN-CORE RECORDS 400 PSIZE NEEDED FOR SIMULATION 218 CALLING PROGRAM NAME:

LOCATED IN: crack3 /home/dutsh5/aio/stock SIMULATION RECUESTED fOR ENTIRE FLOYSHEET

DESCRIPTION

THIS RUN SIMULATES A HYDROCRACKER. fOR THE fIRST STAGE REACTOR,

THE USER DEfINED SUBROUTINE HDSCRA.f IS USED AND THE SECOND STAGE REACTOR USES YLDUSR.F AS SUBROUTINE.

BLOCK STATUS

**.***.*********.*** •••• ** ••••••••••• ***.**** •• ********.*.*****.*.**********

*

* ALL UNIT OPERATION BLOCKS ~ERE COMPLETED NORMALLY

*

* ALL CONVERGENCE BLOCKS ~ERE COMPLETED NORMALLY

* * * * * *.********************************************************.*.**** •• **** •• *** CRACK3.REP 13/08/1993

FLOYSHEET SECTION FLOYSHEET CONNECTIVITY BY STREAMS

STREAM 45 2 59 11 25 31 36 41 5 12A 37 43 47 10 29 27 38 22 18 20 15 12B 120 46 50 4 12F 12H llB 110 56 53 58 NAPHTA DIESEL 3 9 24 33 NA KE DI SOURCE f4 H9 V13 V14 T17 MIXER2 R7A V16 V18 MIXER3 P21 DIVIl T12 DIVI2 C8 DIVI3 DIVI3 DIVI3 MIXER8 MIXER9 H19 V20 P2 MIXERll MIXER12 MIXER13 MIXER14 MULfRAC MULfRAC MULfRAC COOL5 CooL7 DIVI4 H3A Hl0A HllA SEPN SEPK SEPD DEST T17 P2 MULfRAC R6A V13 V14 Hll H19 f5 MIXER8 DIVI2 Hl0 MIXER2 DIVIl MIXER10 MIXER8 MIXER11 MIXER13 R7B R7C V20 H3A R7D R7E R6B R6c P21 CooL7 SEPN SEPD MIXER2 MIXERl H11A HlS

fLOYSHEET CONNECTIVITY BY BLOCKS

BLOCK MIXERl f4 R6A H9 V13 INLETS 9 7 8 11 17 25 STREAM 1 54 8 llA 28 35 40 42 12 32 39 44 52 8B lA 30 34 26 19 21 16 12c 12E 49 51 16A 12G 14 11 C 13 55 60 57 KERO 7 6 17 48 YATERN ~ATERK ~ATERD SOURCE MIXERl R6A V13 V14 H11 T17 fS H15 V16 V18 f22 DIVIl Cl T12 DIVI2 MIXER7 DIVI3 DIVI3 DIVI3 R7B R7c V20 V20 MIXER10 R7D R7E R6B R6C MULfRAC MULfRAC MULfRAC CooL6 DIVI4 DIVI4 H3 Hl0 SEPN SEPK SEPD OUTLETS 8 11 llA 25 28 31 DEST C1 MULfRAC f4 MIXER13 T12 T17 MIXER3 R7A V16 V18 MIXER3 MULfRAC MIXER7 DIVI4 MIXER7 C8 MIXER9 MIXER12 MIXER14 MIXER9 MIXERll DIVI3 MIXER12 Hl0A MIXER14 H3 COOL5 COOL6 SEPK MIXERl MIXER10 H9 f22

(14)

FLOIISHEET V14 Hll T17 MIXER2 F5 R7A H15 V16 V18 MIXER3 F22 P21 DIVll Cl T12 DIVI2 C8 MIXER7 DIVI3 MIXER8 R7B MIXER9 R7C H19 V2D P2 MIXER10 MIXERll R7D MIXER12 R7E MIXER13 R6B MIXER14 R6C MULFRAC CooL5 CooL6 CooL7 DIVI4 H3A H3 Hl0A Hl0 HllA SEPN SEPK SEPD

TIIO STAGE HYDROCRACKER FLOIISHEET SECTION

CONNECTIVITY BY BLOCKS (CONTINUEO) 31 36 40 45 10 3 5 12 33 32 39 42 44 48 53 27 1 28 37 26 8B 34 16A 12A 18 12B 12C 19 120 41 46 2 22 6 12E 20 12F 12G 21 12H 11A 15 11B llc 16 110 52 59 54 55 60 58 lA 4 13 14 47 24 NAPHTA KERO DIESEL 35 36 40 41 42 5 12 12A 32 37 39 43 44 47 52 10 8B 29 lA 27 30 38 34 22 26 18 19 20 21 15 16 129 12C 120 12E 46 49 50 51 4 16A 12F 12G 12H 14 119 11C 110 13 56 55 53 60 58 57 NAPHTA KERO DIESEL 7 3 6 9 17 24 48 33 IIATERN NA IIATERK KE IIATERD Dl

TIIO STAGE HYDROCRACKER FLOIISHEET SECTION CONVERGENCE STATUS SUMMARY

TEAR STREAM SUMMARY

===================

STREAM

10 MAXIMUM ERROR TOLERANCE MAXIMUM ERR/TOL VARIABLE 10

16A .47807E-07 .23115E-05 .20682E-Ol MASS ENTHALPY

44 .46327E-07 .20691E-06 .22391 H2S MOLEFLOII

# = CONVERGEO

* = NOT CONVERGED

CONVERGENCE BLOCK: $OLVER01

TEAR STREAM : 16A 44

TOLERANCE USED: -.500E-03 -.500E-03

TRACE MOLEFRAC: .500E-05 .500E-05

MAXIT= 50 \lAlT 1 ITERATIONS BEFORE ACCELERATING

OMA X = .OOE+OO OMIN = -10.

METHOD: IIEGSTEIN STATUS: CONVERGED

TOTAL NUM9ER OF ITERATIONS: 7

*** FINAL VALUES ***

VARIABLE VALUE PREV VALUE

TOTAL MOLEFLOII KMOL/SEC . 1678467E+01 . 1678464E+01

TOTAL MOLEFLOII KMOL/SEC .2048209E+00 .2048208E+00

F1 MOLEFLOII KMOL/SEC · 6238675E -14 .6271778E-14

F2 HOLEFLOII KMOL/SEC .8555734E-12 .8555121E-12

F3 MOLEFLOII KMOL/SEC .5392031E-l0 .5391922E-10

F4 MOLEFLOII KMOL/SEC . 2235647E-08 .2235635E-08

F5 MOLEFLOII KMOL/SEC .3310212E-07 .33'0196E-07

F6 MOLEFLOII KMOL/SEC .6186507E-06 .6186483E-06

F11 HOLEFLOII KMOL/SEC .1128990E-02 . 1128990E-02

H2 MOLEFLOII KMOL/SEC . 1673588E+01 .1673585E+01

H2S MOLEFLOII KMOL/SEC · 2344440E -02 _2344456E-02

NH3 MOLEFLOII KMOL/SEC .2096155E-03 .2096163E-03

SSC MOLEFLOII KMOL/SEC .OOOOOOOE+OO .OOOOOOOE+OO

NSC MOLEFLOII KMOL/SEC .OOOOOOOE+OO .OOOOOOOE+OO

H20 HOLEFLOII KMOL/SEC . 1779535E-09 . 1778936E - 09

PRESSURE N/SOM • 1200000E+08 . 1200000E+08

MASS ENTHALPY J/KG .4622950E+06 . 4622998E+06

CONV STAT BLOCK # $OLVEROl # $OLVER01 ERR/TOL .3375054E-02 .4353794E-03 -.1055617E+02 _ 1432720E+00 .4037701E-Ol _1016756E-01 .9626098E-02 .7737445E-02 .1464913E-01 .8745612E-02 .5901504E-02 .3414015E-02 .3026939E-03 .3401384E-02 - . 1339253E-01 -.7713081E-02 .OOOOOOOE+OO .OOOOOOOE+OO • 6732659E+00 .OOOOOOOE+OO -.2068209E-01

(15)

TYO STAGE HYOROCRACKER

FL~SHEET SECTION CONVERGENCE BLOCK: SOLVEROl (CONTINUED)

.1550710E-Ol .2824357E-Ol .3194207E-Ol .3589132E-Ol .3261012E-Ol .2187036E-01 • 6472277E-02 .1166929E-02 .4137658E-03 .4665282E-04 .OOOOOOOE+OO .OOOOOOOE+OO .8657519E-09 .5500000E+06 F5 MOLEFL~ KMOL/SEC F6 MOLEFL~ KMOL/SEC F7 MOLEFLOY KMOL/SEC F8 MOLEFLOY KMOL/SEC F9 MOLEFLOY KMOL/SEC Fl0 MOLEFLOY KMOL/SEC Fll MOLEFLOY KMOL/SEC H2 MOLEFLOY KMOL/SEC H2S MOLEFLOY KMOL/SEC NH3 MOLEFLOY KMOL/SEC SSC MOLEFLOY KMOL/SEC NSC MOLEFLOY KMOL/SEC H20 MOLEFLOY KMOL/SEC PRESSURE N/SCM

MASS ENTHALPY J/KG -.267864 7E+06

.1550642E-01 .2824389E-01 .3194196E-Ol .3589129E-Ol .3261008E-Ol .2187033E-Ol .6472269E-02 .1166908E-02 .4138121E-03 .4665585E-04 .OOOOOOOE+OO .OOOOOOOE+OO .8653631E-09 .5500000E+06 -.2678651E+06 ••• ITERATION HISTORY •• * TEAR STREAMS:

ITERAT ION MAX-ERR/TOL STREAM ID VARIABLE

---

--.. ---1 2000. 44 H2 MOLEFLOY 2 2000. 44 H2S MOLEFLOY 3 .3180E+05 44 H2s MOLEFLOY 4 69.13 44 H2S MOLEFLOY 5 1.882 44 H2S MOLEFLOY 6 -1.675 44 H2S MOLEFLOY 7 .8987 44 H20 MOLEFLOY COMPUTATIONAL SECUENCE

---SECUENCE USED YAS:

.8781507E-Ol -.2317518E-Ol .7151387E-02 .1468537E-02 .2313956E-02 .2826271E-02 .2355669E-02 .3583398E-01 -.2239059E+00 -.1296128E+00 .OOOOOOOE+OO .OOOOOOOE+OO . 8986884E+00 .OOOOOOOE+OO .2950769E-02

P2 C1 DIVI4 H3A MIXERl F4 R6A SOLVER01 DIVI3 MIXER13 R6B MIXER14 R6C H3

H9 V13 T12 DIVIl V14 Hll T17 MIXER3 Hl0 F22 MULFRAC P21 HIXER2 F5 R7A MIXER8 R7B MIXER9 R7C MIXER11 R7D MIXER12 R7E H10A H11A H15 V16 DIVI2 MIXER7 C8 MIXER10 V18 SOLVER01<--- H19 V20 CooL7 SEPD COOL6 SEPK COOL5 SEPN

OVERALL FLOYSHEET BALANCE

CRACK3.REP 13/08/1993

TYO STAGE HYDROCRACKER FLOYSHEET SECTION OVERALL FLOYSHEET BALANCE (CONTINUED)

*** HASS AND ENERGY BALANCE ***

IN OUT GENERATION RELATIVE DIFF. CONVENTIONAL COHPONENTS

(KHOL/SEC)

F1 .781875E-02 .145990E-09 -.781875E-02 • 172764E-06 F2 .320777E-01 .885532E-08 - .320777E -01 .321182E-06 F3 .339229E-01 .182547E-05 -.339211E-01 -.662483E -06 F4 .337431E-01 .183182E-02 -.319117E-Ol -.144186E-04 F5 .189644E-01 .381035E-01 .191398E-Ol .178717E-04

F6 .101813E-01 .541674E-01 .439858E-01 - .602735E-05

F7 .OOOOOOE+OO .531314E-01 .531315E-01 .221163E-05 F8 .OOOOOOE+OO .563081E-01 .563081E-01 . 708297E -06 F9 .OOOOOOE+OO .480451E-01 .480451E-01 • 156664E - 05

F10 .OOOOOOE+OO .305796E-01 .305797E-01 .289192E-05 F11 .OOOOOOE+OO .858951E-02 .858953E-02 .184477E-05

H2 .744048 .812959E-01 - .662749 .412927E-05

H2S .OOOOOOE+OO .374252E-Ol .374251E-Ol -.180477E-05 NH3 .OOOOOOE+OO .428358E-02 .428357E-02 -.126860E-05 SSC .374251E-02 .OOOOOOE+OO - .374251E-02 .OOOOOOE+OO

NSC . 214179E -03 .OOOOOOE+OO -.214179E-03 .OOOOOOE+OO

H20 .499584 .499584 .OOOOOOE+OO -. 292539E -06

TOTAL BALANCE

MOLE(KMOL/SEC) 1.38430 .913347 -.470946 .220 136E - 05

MASS(KG/SEC ) 60.5000 60.5000 - .261833E-07 ENTHALPY(YATT - .116591E+08 -.371928E+08 .686522

(16)

PHYSICAL PROPERTIES SECTION

C~PONENTS

---10 TYPE FORMULA NAME OR ALIAS _{REPORT NAME}

F1 C MISSING MISSING F1 F2 C MISSING MISSING F2 F3 C MISSING MISSING F3 F4 C MISSING MISSING F4 F5 C MISSING MISSING F5 F6 C MISSING MISSING F6 F7 C MISSING MISSING _F7 F8 C MISSING MI SSING F8 F9 C MISSING MISSING F9 F10 C MISSING MISSING

_no

F 11 C MISSING MISSING F11 H2 C HZ H2 H2 HZS C HZS H2S H2S NH3 C H3N H3N NH3 SSC C MISSING MISSING SSC NSC C MISSING MISSING NSC H20 C H20 H20 H20

U-O-S BLOCK SECTION

BLOCK: C1 MOOEL: C~PR

INLET STREAM: 1

OUTLET STREAM:

PROPERTY OPTION SET: 1A SYSOP4 PENG-ROBINSON EQUATION OF STATE

••• MASS AND ENERGY BALANCE •••

TOTAL BALANCE

MOLE(KMOL/SEC) MASS(KG/SEC )

ENTHALPY(~ATT

IN OUT RELATIVE DIFF.

.OOOOOOE+OO

-1.00191

GAS PHASE CALCULATION

NO FLASH PERFORMED

.744048 1.50000 -6503.27

••• INPUT DATA •••

TYPE: ISENTROPIC CENTRIFUGAL COMPRESSOR

OUTLET PRESSURE N/SQM

ISENTROPIC EFFICIENCY

MECHANICAL EFFICIENCY

••• RESULTS *** INDICATED HORSEPO~ER REQUIREMENT ~ATT

BRAKE HORSEPO~ER REQUIREMENT ~ATT

NET ~RK, ~ATT

ISENTROPIC HORSEPO~ER REQUIREMENT ~ATT

CAL CU LAT EO OUTLET TEMP K

ISENTROPIC TEMPERATURE K

OUTLET VAPOR FRACTION

BLOCK: C8 MOOEL: C~PR INLET STREAM: 26 OUTLET STREAM: .744048 1.50000 .339840E+07 0.120000+08 0.72000 1.00000 3,404,900. 3,404,900. -3,404,900. 2,451,530. 454.598 410.898 1.00000

PROPERTY OPTION SET: 22 SYSOP4 PENG-ROBINSON EQUATION OF STATE

TOTAL BALANCE

ENTHALPY(~ATT

*** MASS AND ENERGY BALANCE .*.

IN OUT 1.52966 3.34104 653580. 1.52966 3.34104 .100353E+07 RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO - .348719

(17)

U-O-S BLOCK SECTION

BLOCK: C8 MODEL: COHPR (CONTINUEO)

GAS PHASE CALCULATION

NO FLASH PERFORMED

*** INPUT DATA ***

TYPE: ISENTROPIC CENTRIFUGAL COMPRESSOR

OUTLET PRESSURE N/SOM

ISENTROPIC EFFICIENCY

MECHANICAL EFFICIENCY

*** RESULTS ***

INDICATED HORSEPOYER REOUIREMENT ~ATT

BRAKE HORSEPOYER REOUIREMENT ~ATT

NET ~ORK, ~ATT

ISENTROPIC HORSEPOYER REOUIREMENT ~ATT

CALCULATED OUT LET TEMP K

ISENTROPIC TEMPERATURE K

OUTLET VAPOR FRACTION

BLOCK: coaL5 MODEL: HEATER

INLET STREAM: OUTLET STREAM: 0.120000+08 0.72000 1.00000 349,950. 349,950. -349,950. 251,964. 320.903 318.715 1.00000

PROPERTY OPTION SET:

55

NAPHTA

SYSOP4 PENG-ROBINSON EOUATION OF STATE

*** MASS AND ENERGY BALANCE ***

TOTAL BALANCE MOLE(KMOL/SEC)

MASS(KG/SEC )

ENTHALPY(~ATT

T~O PHASE TP FLASH

SPECIFIED TEMPERATURE SPECIFIED PRESSURE

MAXIMUM NO. ITERATIONS

CONVERGENCE TOLERANCE *** CRACK3.REP 13/08/1993 IN OUT RELATIVE DI FF. .OOOOOOE+OO -.126099E-15 .174244 .723517E-Ol 7.04353 - .206954E+07 INPUT DATA *** K N/SOM .723517E-Ol 7.04353 - .250623E+07 298.150 100,000. 30 0.00010000

U-O-S BLOCK SECTION

BLOCK: CoaL5 MODEL: HEATER (CONTINUEO)

OUTLET TEMPERATURE OUTLET PRESSURE

HEAT DUTY VAPOR FRACT ION

VOl PHASE EOUILIBRIUM COMP F6 F7 F8 F9 Fl0 Fll H2 H2S NH3 H20 *** RESULTS *** K N/SQM ~ATT F (I) .18137E-09 .17910E-04 .12948E-Ol .54282 .30979 .79344E-Ol .30285E-03 .23100E-02 .30053E-03 .52168E-Ol X( I) .18137E-09 .17910E-04 .12948E-Ol .54282 .30979 .79344E-Ol .30285E-03 .23100E-02 .30053E-03 .52168E-Ol

BLOCK: coaL6 MODEL: HEATER INLET STREAM: OUTLET STREAM: 298.15 .10000E+06 -.43670E+06 .OOOOOE+OO Y( I) .48016E-14 .71897E-08 .58446E-04 .21404E-Ol .86513E-Ol .13198 .58899 .65039E-Ol .59622E-02 .10006 K(I) .16600E-04 .25172E-03 .28303E-02 .24724E-Ol .17510 1.0430 1219.4 17 .653 12.439 1.2026

60

KERO

SYSOP4 PENG-ROBINSON EOUATION OF STATE

TOTAL BALANCE

ENTHALPY( ~A TT

***

T~O PHASE TP FLASH

CONVERGENCE TOLERANCE

MASS AND ENERGY BALANCE ***

.OOOOOOE+OO .OOOOOOE+OO .629306 .104982 16.0000 - . 192661E+07 *** INPUT DATA *** K N/SOM .104982 16.0000 -.519731E+07 298.150 100,000. 30 0.00010000

(18)

T~O STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: CODL6 MODEL: HEATER (CONTINUEDl

••• RESULTS ••• OUTLET TEMPERATURE OUTLET PRESSURE HEAT DUTY VAPOR fRACTION K N/SQM ~ATT V-L PHASE EQUILIBRIUM: COMP f ( I l f4 .64281E-10 f5 .24403E-05 f6 .33941E-02 f7 .38696 f8 .51100 f9 .42973E-Ol fl0 .20375E-03 fll .23082E-05 H2 .29843E-ll H2S .88768E-09 NH3 .12872E-09 H20 .55457E-Ol

BLOCK: COOL7 MODEL: HEATER

---

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

-

---- -- -- - --. INLET STREAM: OUTLET STREAM: X([l .64281E-10 .24403E-05 .33941E-02 .38696 .51100 .42973E-01 .20375E-03 .23082E-05 .29843E-ll .88768E-09 .12872E-09 .55457E-Ol 298.15 .1DDOOE+06 -.32707E+07 .OOOOOE+OO Y( I l K([l .15343E-16 .20680E-07 .18662E-10 .66258E-06 _58549E-06 .14946E-04 .10625E-02 .23789E-03 .16485E-Ol .27950E-02 .12552E-Ol .25307E-Ol .43206E-03 .18372 .29478E-04 1.1065 .35275E-07 1024.1 .18800E-06 18.350 .19903E-07 13.396 .96944 1.5145

PROPERTY OPTION SET: 58

DIESEL

SYSOP4 PENG-ROBINSON EQUATION Of STATE ••• MASS AND ENERGY BALANCE •••

TOTAL BALANCE MOLE(KMOL/SECl MASS(KG/SEC l

ENTHALPY(~ATT

T~O PHASE TP fLASH SPEClflED TEMPERATURE SPEClflED PRESSURE MAXIMUM NO. ITERATIONS CONVERGENCE TOLERANCE

•••

IN OUT RELATIVE Dlff. .OOOOOOE+OO .OOOOOOE+OO 1.32635 .108321 25.5000 .250183E+07 INPUT DATA ... K N/SQM .108321 25.5000 -.766617E+07 298.150 100,000. 30 0.00010000

T~O STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: CooL7 MODEL: HEATER (CONTINUEDl

••• RESULTS ••• OUTLET TEMPERATURE

OUTLET PRESSURE HEAT DUTY VAPOR fRACT ION

K N/SQM ~ATT V-L PHASE EQUILIBRIUM: COMP f([ l fl .21663E-ll f2 .95784E-08 f3 .15539E-04 f4 .16894E-Ol f5 .35164 f6 .49603 f7 .11236 f8 .30512E-02 f9 .17507E-03 fl0 .83700E-05 fl1 .25947E-06 H2 .11683E-l0 H2S .38866E-09 NH3 .45305E-l0 H20 .19828E-Ol

BLOCK: D lVI 1 MODEL: fSPL I T

---

.. ---INLET STREAM: 27 OUTLET STREAMS: X([l .21663E-ll .95784E-08 • 15539E - 04 .16894E-Ol .35164 .49603 .11236 .30512E-02 .17507E-03 .83700E-05 .25947E-06 .11683E-10 .38866E-09 .45305E-l0 . 19828E -01 29 298.15 _10000E+06 -.10168E+08 _OOOOOE+OO Y([l K( I l .36922E-23 .58833E-13 .10710E-17 .38597E-ll .18169E-12 .40360E-09 .94851E-08 .19380E-07 .64020E-05 .62844E-06 .20838E-03 .14501E-04 .76859E-03 .23612E-03 .25035E-03 .28322E-02 . 13225E -03 .26076E-Ol .46401E-04 .19136 .86941E-05 1.1566 .31583E-06 933.14 .21275E-06 18.895 .18468E-07 14.071 .99858 1.7384

PROPERTY OPTION SET: 8B SYSOP4 PENG-ROBINSON EQUATION Of STATE

TOTAL BALANCE MOLE(KMOL/SECl MASS(KG/SEC l ENTHALPY(~ATT fRACTION Of fLO~ STREAM= 8B 29

•••

MASS AND ENERGY BALANCE

• ••

IN OUT .405323 .405323 .885305 .885305 172696. 172696.

• ••

INPUT DATA

• ••

STRM=29 fRAC=

•••

RESULTS

• ••

SPLl T= 0.95000 KEY= 0.050000 0 0 RELATIVE Dlff. .OOOOOOE+OO .OOOOOOE+OO .OOOOOOE+OO 0.050000

(19)

BLOCK: DIVI2 INLET STREAM: OUTLET STREAMS:

TYO STAGE HYDROCRACKER U-O-S BLOCK SECTION MODEL: FSPLlT

37

34

PROPERTY OPTION SET: 38 SysoP4 PENG-ROBINSON EQUATION OF STATE

•••

MASS AND ENERGY BALANCE

• ••

IN OUT TOT AL BALANCE MOLE(KMOL/SEC) 1.15605 1. 15605 MASS(KG/SEC ) 2.52501 2.52501 ENTHALPY(IJATT 494438. 494438.

•••

INPUT DATA

• ••

MASS-FLOIJ (KG/SEC ) STRM=34 FLOIJ=

•••

RESULTS

• ••

STREAM= 38 SPLIT= 0.0099032 KEY=

34 0.99010

BLOCK: DIVI3 MODEL: FSPLlT

---INLET STREAM: 16A

OUT LET STREAMS: 18 19 20

0 0 RELATIVE OIFF. .OOOOOOE+OO .OOOOOOE+OO .OOOOOOE+OO 2.50000 KEY= 0 21 15 16

PROPERTY OPTION SET: SYSOP4 PENG-ROBINSON EQUATION OF STATE

•••

MASS ANO ENERGY BALANCE

• ••

TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPY(IJATT MASS-FLOIJ (KG/SEC

•••

CRA CK3.REP 13/08/1993 IN 1.67847 3.64104 .168193E+07 INPUT DATA

• ••

STRM=19 STRM=20 STRM=21 STRM=15 STRM=16 OUT 1.67846 3.64103 .168197E+07 FLOIJ= FLOIJ= FLOIJ= FLOIJ= FLOIJ= RELATIVE OIFF. .179337E-05 .148690E-05 -.239510E-04 0.66000 KEY= 0 0.66000 KEY= 0 0.66000 KEY= 0 0.50000 KEY= 0 0.50000 KEY= 0

TIJO STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: OIV!3 MODEL: FSPLIT CCONTINUEO)

•••

RESULTS

• ••

STREAM= 18 SPLI T= 0.18155 KEY= 0

19 0.18127 0

20 0.18127 0

21 0.18127 0

15 0.13732 0

16 0.13732 0

BLOCK: 0lVI4 MODEL: FSPLl T

---INLET STREAM: 1A

OUTLET STREAMS: 7 3 6

PROPERTY OPTION SET: SYSOP4 PENG-ROBINSON EQUATION OF STATE ••• MASS ANO ENERGY BALANCE •••

IN OUT

TOTAL BALANCE

MOLECKMOL/SEC) .744048 .744048 MASSCKG/SEC ) _1.50000 _1.50000

ENTHALPYCIJATT .339840E+07 .339840E+07

•••

INPUT DATA

• ••

MASS-FLOIJ (KG/SEC ) STRM=7 FLOIJ= STRM=3 FLOIJ=

•••

RESULTS

.*.

STREAM= 7 SPLlT= 0.33333 KEY= 0

3 0.46667 0

6 0.20000 0

BLOCK: F22 MODEL: HEATER INLET STREAM: 48 OUTLET STREAM: RELATlVE OIFF. _OOOOOOE+OO .148030E-15 .OOOOOOE+OO 0.50000 0.70000 KEY= 0 KEY= 0

TOTAL BALANCE MOLECKMOL/SEC) MASSCKG/SEC ) ENTHALPY(IJATT

••• MASS ANO ENERGY BALANCE

***

IN OUT .453541 87.7812 . 262243E+08 .453541 87.7812 .436292E+08 RELATlVE DIFF. .OOOOOOE+OO .OOOOOOE+OO - .398929

(20)

~

-TYO STAGE HYDROCRACKER

U-O-S BLOCK SECTION

BLOCK: F22 MODEL: HEATER (CONTINUED)

*** INPUT DATA ***

TYO PHASE TP FLASH

CONVERGENCE TOLERANCE K 603.150 OUTLET TEMPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACT I ON V-L PHASE ECUILIBRIUH COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 F10 F11 H2 H2s NH3 H20 N/SCH 500,000. *** RESUL TS *** K N/SCM YATT F ( I ) .10757E-01 .48244E-01 .63907E-01 .10228 .90930E-01 .11956 .11643 .12108 .97031E-01 .50836E-01 .14271E-01 .25729E-02 .91240E-03 .10287E-03 .16108 X( I) .23891E-01 .10603 .13583 .20058 .15109 .15064 .10039 .67029E-01 .33710E-01 .11096E-01 .19885E-02 .61528E-04 .55963E-04 .61322E-05 .17593E-01 30 0.00010000 603.15 .50000E+06 .17405E+08 .55187 Y( I) K(I) .92050E-04 .38529E-02 • 13200E -02 .12450E-01 .55026E-02 .40511E-01 .22458E-01 .11196 .42074E-01 .27847 .94321E-01 .62612 .12945 1.2895 .16497 2.4612 .14845 4.4038 .83107E-01 7.4901 .24244E-01 12.192 .46122E-02 74.961 .16079E-02 28.731 .18142E-03 29.586 .27760 15.779

BLOCK: F4 MODEL: HEATER

1 NLET STREAH:

OUTLET STREAM: PROPERTY OPTION SET:

8

11

Sysop4 PENG-ROBINSON ECUATION OF STATE *** MASS ANO ENERGY BALANCE ***

TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPY(YATT IN OUT .388681 50.5000 . 249963E+08 .388681 50.5000 .321113E+08 RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO -.221571

U-O-S BLOCK SECTION

BLOCK: F4 MODEL: HEATER (CONTINUED)

*** INPUT DATA

***

TYO PHASE TP FLASH

CONVERGENCE TOLERANCE K 658.150 N/SCH 0.119000+08 *** RESULTS *** OUTLET TEHPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACT ION

V-L PHASE ECUILIBRIUH COMP F1 F2 F3 F4 F5 F6 H2 SSC NSC K N/SCH YATT F(I ) .20116E-01 .82530E-01 .87277E-01 .86814E-01 .48792E-01 .26195E-01 .63810 .96288E-02 .55104E-03

BLOCK: F5 MODEL: HEATER

---INLET STREAM: 5 OUTLET STREAH: X( I) .42513E-01 .17391 _ 18258 .17901 .97967E-01 .50328E-01 .25241 .20139E-01 .11371E-02 30 0.00010000 658.15 .11900E+08 .71149E+07 .52774 Y ( I ) K(I ) .73528E-04 .17295E-02 .75894E-03 .43641E-02 .19900E-02 .1 0899E -01 .43068E-02 .24058E-01 .47859E-02 .48852E-01 .45980E-02 .91361E-01 .98324 3.8954 .22349E-03 .11097E-01 .26617E-04 .23408E-01

PROPERTY OPTION SET: SYSOP4 12 PENG-ROBINSON ECUATION OF STATE

*** HASS AND ENERGY BALANCE ***

TOTAL BALANCE

HOLE(KHOL/SEC) MASS(KG/SEC )

ENTHALPY(YATT

TYO PHASE TP FLASH

***

.OOOOOOE+OO .OOOOOOE+OO .256383E-02 .450822 38.7000 . 256982E+08 INPUT DATA K N/SCH *** .450822 38.7000 .256323E+08 653.150 0.119000+08 30 0.00010000

(21)

TIIO STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: F5 MODEL: HEAT ER (CONTINUED)

*** RESULTS *** OUTLET TEMPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACTION V-L PHASE EQUILIBRIUM COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 Fl0 Fll H2 H2S NH3 H20 K N/SQM IIATT F ( I ) .10822E-Ol .48535E-Ol .64288E-Ol .98840E-Ol .69865E-02 .30960E-03 .19291E-04 .17771E-05 .16056E-06 .11538E-07 .52676E-09 .77020 .13492E-ll . 13050E -12 .21546E-08 BLOCK: Hl0 MODEL: HEATER

---._---INLET STREAM: 47 OUTLET STREAM: X(I) .36357E-Ol .16221 .21204 .31742 .21351E-Ol .87224E-03 .48182E-04 .37772E-05 .27942E-06 .15944E-07 .56653E-09 .24970 .85195E-12 .79883E-13 .19974E-08 653.15 .11900E+08 -65886. .70331 Hl) K( I) .50324E-04 . 13842E-02 .58260E-03 .35917E -02 .19583E-02 .92355E-02 .66343E-02 .20901E-Ol .92677E-03 .43406E-Ol .72258E-04 .82841E-Ol .71029E-05 .14742 .93334E-06 .24710 .11042E-06 .39518 .96798E-08 .60711 .50999E-09 .90020 .98977 3.9639 .15589E-ll 1.8298 .15186E-12 1. 9010 .22209E-08 1.1119

MASS(KG/SEC ) ENTHALPHIIATT TIIO PHASE TP FLASH

MAXIMUM NO. ITERATIONS CONVERGENCE TOLERANCE *** CRACK3.REP 13/08/1993 IN OUT RELATIVE DI FF. .OOOOOOE+OO .OOOOOOE+OO -1.57810 .453541 87.7812 -.151602E+08 INPUT DATA K N/SQM *** .453541 87.7812 .262243E+08 543.150 400,000. 30 0.00010000 T~ STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: Hl0 MODEL: HEATER (CONTINUEO)

*** RESULTS *** OUTLET TEMPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACT I ON K N/SQM IIATT V-L PHASE EQUILIBRIUM: COMP Fe I) Fl .10757E-Ol F2 .48244E-Ol F3 .63907E-Ol F4 .10228 F5 .90930E-Ol F6 .11956 F7 .11643 F8 .12108 F9 .97031E-Ol Fl0 .50836E-Ol Fll .14271E-Ol H2 .25729E-02 H2S .91240E-03 NH3 .10287E-03 H20 .16108

BLOCK: H1DA MOOEL: HEATER

._._---INLET STREAM: 14 OUTLET STREAM: 24 X(I) .17486E-Ol .78354E-Ol .10338 .16328 .13960 .16668 .13349 .10080 .52623E-Ol .16861E-Ol .28270E-02 .56962E-04 .67990E-04 .75964E-05 .24491E-Ol 543.15 .40000E+06 .41384E+08 .38498 Y(I) K(I) .71563E-05 .40926E-03 .14007E-03 . 17876E-02 .83885E-03 .81138E-02 .48325E-02 .29596E-Ol .13183E-Ol .94438E-Ol .44290E-Ol .26572 .89171E-Ol .66800 .15349 1.5227 .16798 3.1921 .10511 6.2344 .32552E-Ol 11.515 .65922E-02 115.73 .22614E-02 33.261 .25508E-03 33.578 .37930 15.488

PROPERTY OPTION SET: SYSOP4 PENG-ROBINSON EQUATION OF STATE

MASS(KG/SEC ) ENTHALPY(IIATT TIIO PHASE TP FLASH

MAXIMUM NO. ITERATIONS CONVERGENCE TOLERANCE

***

IN OUT RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO .924463 1.38484 41.3410 .457708E+08 INPUT DATA K N/SQM *** 1.38484 41.3410 .345740E+07 423.150 0.113800+08 30 0.00010000

(22)

U-O-S BLOCK SECTION

BLOCK: H10A MODEL: HEATER (CONTINUED)

*** RESULTS *** OUTLET TEMPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACTION V-L PHASE EQUILIBRIUM COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 Fl0 Fll H2 H2S NH3 H20 K N/SQM IIATT F( I) .56383E-03 .30091E-02 .55280E-02 .13036E-01 .11198E-Ol .20395E-Ol .23070E-Ol .25953E-01 .23748E-Ol .16499E-01 . 56424E -02 .85002 .12280E-02 .10979E-03 . 79459E -09

BLOCK: H11 MOOEL: HEATER

---INLET STREAM: 36

OUT LET STREAM:

XCI) .35707E-02 .19057E-01 .35008E-01 .82545E-01 .70848E-01 .12860 .14364 .15536 .12828 .71457E-Ol . 16735E -Ol .14349 .12895E-02 .12241E-03 .20182E-08 423.15 . 11380E+08 -.42313E+08 .84209 Y(I) K( I) .20014E-09 .56050E-07 .90111E-08 .47286E-06 .16298E-06 .46555E-05 .26216E-05 .31760E-04 .12560E-04 • 17728E-03 .10571E-03 .82205E-03 .46182E-03 .32152E-02 .16863E-02 .10854E-01 .41470E-02 .32328E-Ol .61938E-02 .86679E-Ol .35624E-02 .21287 .98250 6.8470 .12164E-02 .94331 .1 0743E - 03 .87758 .56515E-09 .28003

*** MASS AND ENERGY BALANCE ***

TOTAL BALANCE

ENTHALPY(~ATT

T~O PHASE TP FLASH

CONVERGENCE TOLERANCE *** IN OUT .204597 49.6529 -.131089E+08 INPUT DATA *** .204597 49.6529 -.553984E+07 RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO - .577399 K 393.150 N/SQM 500,000. 30 0.00010000

TWO STAGE HYDROCRACKER U-O-S BLOCK SECTION

BLOCK: H11 MODEL: HEAT ER (CONTINUED)

*** RESULTS *** OUTLET TEHPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACTION K N/SQM ~ATT V-L.PHASE EQUILIBRIUM: COMP F ( I ) F1 .20030E-01 F2 .86577E-01 F3 .10425 F4 .13850 F5 .12584 F6 .12739 F7 .10360 F8 .99715E-01 F9 .74967E-01 F10 .40850E-01 F11 .81424E-02 H2 .34883E-02 H2S .58504E-01 NH3 .81454E-02 H20 .19921E-09

BLOCK: H11A MODEL: HEATER

---INLET STREAM: 24 OUTLET STREAM: XCI ) .20282E-01 .87667E-01 .10556 .14025 .12743 .12899 .10489 .10091 .75725E-01 .41014E-01 .80326E-02 .12251E-02 .50851E-01 .71824E-02 • 19439E-09 393.15 .50000E+06 .75691E+07 .12434E-01 YCI) KCI) .21162E-09 .10434E-07 .13195E-07 .15052E-06 .28288E-06 .26797E-05 .42225E-05 .30108E-04 .33621E-04 .26385E-03 .23844E-03 _18486E-02 .10955E-02 .10445E-01 .49367E-02 .48923E-01 .14770E-01 .19505 • 27813E -01 .67815 .16864E-01 2.0995 .18324 149.57 .66637 13.104 .84636E-01 11. 784 .58268E-09 2.9975

TOTAL BALANCE

ENTHALPY(~ATT

TIIO PHASE TP FLASH

CONVERGENCE TOLERANCE *** IN OUT 1.38484 41.3410 .345740E+07 INPUT DATA *** 1.38484 41.3410 -.412844E+07 RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO 1.83746 K 363.150 N/SQM 0.113500+08 30 0_00010000

(23)

TUO STAGE HYDROCRACKER U-O-S BlOCK SECTION

BlOCK: HllA MODEL: HEAT ER (CONTINUED) ••• RESUlTS ••• OUTLET TEMPERATURE

OUlLET PRESSURE HEAT DUTY VAPOR FRACT ION

VOl PHASE EQUILIBRIUM COMP Fl F2 F3 F4 F5 F6 F7 F8 F9 Fl0 Fll H2 H2s NH3 H20 K N/SQM IIATT F (I) .56383E-03 .30091E-02 .55280E-02 .13036E-Ol .11198E-Ol .20395E-Ol .23070E-Ol .25953E-Ol .23748E-Ol .16499E-Ol .56424E -02 .85002 .12280E-02 .10979E-03 .79459E-09

BlOCK: H15 MODEL: HEATER

---

.

---INlET STREAM: 33 OUlLET STREAM: X(I) .34349E-02 .18332E-Ol .33677E-Ol .79417E-Ol .68214E-Ol .12421 .14028 .15666 .13936 .88319E-Ol .23789E-Ol .12223 .18938E-02 .18903E-03 .30719E-08 363.15 .11350E+08 - .75858E+07 .83585 Y( I) K( I) .76892E-12 .22386E-09 .64132E-l0 .34984E-08 .24001E-08 .71268E-07 .69615E-07 .87658E-06 .56576E-06 .82939E-05 .76760E-05 .61800E-04 .51605E-04 .36788E-03 .28254E-03 .18034E-02 .10444E-02 .74948E-02 .23948E-02 .27115E-Ol .20786E-02 .87376E-Ol .99295 8.1236 .10972E-02 .57938 .94232E-04 .49850 .34735E-09 .11307

PROPERTY OPTION SET: 32 SYSOP4 PENG-ROBINSON EQUATION OF STATE •• * MASS ANO ENERGY BAlANCE ***

TOTAl BAlANCE

MOlE(KMOL/SEC) MASS(KG/SEC ) ENTHAlPY(IIATT TIIO PHASE TP FLASH

MAXIMUM NO. ITERATIONS CONVERGENCE TOlERANCE *** CRA CK3.REP 13/08/1993 IN OUT 1.38484 41.3410 -.412844E+07 INPUT DATA *** 1.38484 41.3410 -.986101E+07 RElATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO .581337 K 313.150 N/SQM 0.113000+08 30 0.00010000

TUO STAGE HYDROCRACKER U-O-S BLOCK SECTION

BlOCK: H15 MODEL: HEATER (CONTINUED) ••• RESULTS ••• OUTLET TEMPERATURE

OUTLET PRESSURE HEAT DUTY VAPOR FRACTION

VOl PHASE EQUILIBRIUM COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 F10 F11 H2 H2S NH3 H20 K N/SQM IIATT F ( I ) .56383E-03 .30091E-02 .55280E-02 .13036E-Ol .11198E-Ol .20395E-Ol .23070E-Ol .25953E-Ol .23748E-Ol .16499E-Ol .56424E-02 .85002 .12280E-02 .10979E-03 .79459E-09

BlOCK: H19 MODEL: HEATER

---INlET STREAM: 41 OUlLET STREAM: X(I) .34129E-02 .18214E-Ol .33461E-Ol .78909E-Ol .67780E-Ol .12345 .13962 .15691 .14276 .96477E-Ol .29599E-Ol .10625 .28626E-02 .29703E-03 .40375E-08 313.15 .11300E+08 -.57326E+07 .83479 Y( I) K(I) .14261E-14 .41787E-12 .23667E-12 .12994E-10 .20249E-l0 .60516E-09 .11431E-08 .14486E-07 .16863E-07 .24879E-06 .39138E-06 .31703E-05 .42364E-05 .30342E-04 .35572E-04 .22671E-03 .19588E-03 .13721E-02 .67138E-03 .69590E-02 .90129E-03 .30450E-Ol .99721 9.3854 .90450E-03 .31598 .72739E-04 .24489 .15280E-09 .37845E-Ol

PROPERTY OPTION SET: 46 SYSOP4 PENG-ROBINSON EQUATION OF STATE *.* MASS AND ENERGY BAlANCE ***

TOTAl BALANCE

MOlE(KMOl/SEC) MASS(KG/SEC ) ENTHALPY(IIATT TIIO PHASE TP FLASH

SPECIFIEO TEMPERATURE SPECIFIED PRESSURE

MAXIMUM NO. ITERATIONS CONVERGENCE TOlERANCE *** IN OUT .233423 5.58962 986083. INPUT DATA *** .233423 5.58962 -.928088E+07 RElATIVE OIFF. .OOOOOOE+OO .OOOOOOE+OO 1. 10625 K 303.150 N/SQM 500,000. 30 0.00010000

(24)

TIJO STAGE HYOROCRACKER

U-O-S BLOCK SECTION

BLOCK: H19 MODEL: HEATER (CONTINUEO)

*** RESULTS ***

OUT LET TEMPERATURE

OUTLET PRESSURE

HEAT DUTY

VAPOR FRACTION

VOl PHASE EQUILIBRIUM

COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 F10 F11 H2 H2S NH3 H20 K N/SQM IJATT F ( I ) .62443E-09 .33492E-07 .60933E-06 .78910E-05 .55156E-04 .34601E-03 .14278E-02 .59020E-02 .16882E-01 .30724E-01 .71366E-02 .30575E-02 .51280E-01 .71396E-02 .87604

BLOCK: H3 MODEL: HEATER

---

--

---

--

---INLET STREAM: 13 OUTLET STREAM: X( I ) .58020E-29 .40960E-27 .99082E-26 .16494E-24 .14514E-23 .11308E-22 .11229E-21 .28129E-16 .11187E-11 .54751E-08 .57933E-06 .46223E-07 .18769E-02 .20129E-02 .99611 303.15 .50000E+06 - . 10267E+08 .12147 Y (I) K(I) .51407E-08 .88602E+21 . 27573E -06 .67316E+21 .50164E-05 .50628E+21 .64964E-04 .39387E+21 .45408E-03 .31285E+21 .28486E-02 .25191E+21 .11754E-01 .10468E+21 .48589E-01 .17274E+16 .13898 .12424E+12 .25294 .46199E+08 .58749E-01 .10141E+06 .25171E-01 .54455E+06 .40859 217.69 .44219E-01 21.967 .76317E-02 .76615E-02

PROPERTY OPTION SET: 17 Sysop4 PENG-ROBINSON EQUATION OF STATE *** MASS AND ENERGY BALANCE ***

TOTAL BALANCE

ENTHALPY(IJATT

TIJO PHASE TP FLASH

***

.OOOOOOE+OO .OOOOOOE+OO .910940 .662184 51.5000 .416927E+08 INPUT DATA K N/SQM *** .662184 51.5000 .371313E+07 450.150 0.113500+08 30 0.00010000

TIJD STAGE HYDRDCRACKER U-O-S BlOCK SECTION

BLOCK: H3 MODEL: HEAT ER (CONTINUED)

*** RESULTS ***

OUTLET TEHPERATURE OUTLET PRESSURE HEAT DUTY VAPOR FRACTION

COMP F1 F2 F3 F4 F5 F6 F7 F8 F9 F10 F11 H2 H2S NH3 H20 K N/SQM IJATT F(I) .61886E-02 .26750E-01 .32210E-01 .42794E-01 .38882E-01 .39359E-01 .32013E-01 .30835E-01 .23289E-01 . 12998E-01 .28763E-02 .64776 .57490E-01 .65558E-02 .73783E-10

BLOCK: H3A MODEL: HEATER

---INLET STREAM: 4

OUT LET STREAM:

X(I ) . 17639E-01 .76244E-01 .91804E-01 .12195 .11070 .11172 .90010E-01 .84503E-01 .60086E-01 .29640E-01 .52802E-02 .14134 .52853E-01 .62291E-02 .12246E-09 450.15 • 11350E+08 - .37980E+08 .64916 Y(I) K(I) .83329E-08 .47241E-06 .23892E-06 .31336E-05 .21511E-05 .23432E-04 .15537E-04 .12741E-03 .64200E-04 .57993E-03 .24975E-03 .22355E-02 . 66788E-03 .74200E-02 .18293E-02 .21647E-01 .34012E-02 .56606E-01 .40034E-02 .13507 .15771E-02 .29868 .92146 6.5195 .59996E-01 1. 1351 .67323E-02 1.0808 .47473E-10 .38765

PROPERTY OPTION SET: 9 SysOP4 PENG-ROBINSON EQUATION OF STATE

TOTAL BALANCE

ENTHALPY<IJATT TIJO PHASE TP FLASH

SPECIFIED TEMPERATURE SPECIFIEO PRESSURE

***

IN OUT RELATIVE OIFF.

.OOOOOOE+OO .OOOOOOE+OO -1.58218 .140665 50.0000 -.138929E+08 INPUT DATA K N/SQM *** .140665 50.0000 . 238636E+08 623.150 0.118500+08 30 0.00010000

(25)

T~ STAGE HYDROCRACKER

U-O-S BLOCK SECTION

BLOCK: H3A MODEL: HEATER (CONTINUED) *** RESULTS *** OUTLET TEMPERATURE

OUTLET PRESSURE HEAT DUn VAPOR FRACTION

COMP Fl F2 F3 F4 F5 F6 SSC NSC K N/SQM ~ATT F ( I ) .55584E-01 .22804 .24116 .23988 .13482 .72380E-Ol .26606E-01 .15226E-02

BLOCK: H9 MODEL: HEATER

---INLET STREAM: 17 OUTLET STREAM: X(I) .55584E-Ol .22804 .24116 .23988 .13482 .72380E-Ol .26606E-Ol .15226E-02 623.15 .11850E+08 .37757E+08 .OOOOOE+OO Y ( I ) K(I) .74031E-02 .27468E-02 .64185E-Ol .57955E-02 .14541 . 12396E -Ol .27273 .23340E-Ol .26743 .40670E-Ol .22968 .64984E-Ol .11848E-Ol .91483E-02 .13195E-02 .17782E-Ol

IN OUT TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPY(~A TT .662184 51.5000 .371313E+07 .662184 51.5000 -.129282E+08 RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO 1.28721

T~O PHASE TP FLASH

SPECIFIED TEMPERATURE SPECIFIED PRESSURE MAXIMUM NO. ITERATIONS

CONVERGENCE TOLERANCE *** CRACK3.REP 13/08/1993 INPUT DATA K N/SQM *** 313.150 0.113000+08 30 0.00010000 T~ STAGE HYDROCRACKER

U-O-S BLOCK SECTION

BLOCK: H9 MODEL: HEATER (CONTINUED)

*** RESULTS *** OUTLET TEMPERATURE OUTLET PRESSURE HEAT Dun VAPOR FRACTION K N/SQM ~ATT

VOl PHASE EQUILIBRIUM:

COMP F(I ) F1 .61886E-02 F2 .26750E-01 F3 .32210E-01 F4 .42794E-01 F5 .38882E-01 F6 .39359E-01 F7 .32013E-01 F8 .30835E-01 F9 .23289E-01 Fl0 .12998E-01 F11 .28763E-02 H2 .64776 H2S .57490E-Ol NH3 .65558E-02 H20 .73783E-l0

BLOCK: MIXERl MODEL: MIXER

._---INLET STREAMS: 9 OUTLET STREAM: X(I) .16846E-01 .72816E-01 .87679E-01 .11649 .10584 .10714 .87137E-01 .83897E-01 .63224E-01 .34916E-01 .74083E-02 .10439 .99845E-01 .12378E-Ol .18761E-09 7 313.15 .11300E+08 - .16641E+08 .63264 Y(I) K(I) .11575E-13 .68710E-12 .14692E-11 .20177E-10 .77250E-10 .88106E-09 .23300E-08 .20002E-07 .34678E-07 .32765E-06 .42887E-06 .40029E-05 .32159E-05 .36906E-04 .22377E-04 .26672E-03 .99064E-04 . 15669E-02 .27009E-03 .77354E-02 .24465E-03 .33024E-Ol .96329 9.2282 .32895E-Ol .32946 .31750E-02 .25651 .76842E-11 .40958E-Ol

TOTAL BALANCE

ENTHALPY(\lATT

***

T~O PHASE FLASH

MASS AND ENERGY BALANCE ***

IN OUT .388681 50.5000 .249964E+08 *** INPUT DATA *** .388681 50.5000 . 249963E+08

OUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES

RELATIVE DIFF. .OOOOOOE+OO .422105E-15 .310790E-05 30 0.00010000

(26)

TWO STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: MIXER10 MODEL: MIXER

INLET STREAMS: 22 6

OUTLET STREAM:

PROPERTY OPTION SET: 16A SYSOP4 PENG-ROBINSON EQUATION OF STATE

TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPY(IIATT

*""

TIIO PHASE FLASH MAXIMUM NO. ITERATIONS CONVERGENCE TOLERANCE

MASS AND ENERGY BALANCE "**

IN OUT 1.67847 3.64104 .168321E+07 "*" INPUT DATA *** 1.67847 3.64104 .168193E+07

OUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES BLOCK: MIXER11 MODEL: MIXER

INLET STREAMS: 20 OUTLET STREAM: RELATIVE DIFF. .OOOOOOE+OO .243935E-15 .759151E-03 30 0.00010000

12E 12F

SYSOP4 PENG-ROBINSON EQUATION OF STATE

***

MASS AND ENERGY BALANCE "**

IN OUT 1.17456 40.6810 .387734E+08 "** INPUT DATA *** 1.17456 40.6810 .387746E+08

INLET STREAMS: 21 OUTLET STREAM: RELATIVE DIFF. .OOOOOOE+OO .698648E-15 - .302937E-04 30 0.00010000

PROPERTY OPTION SET: 12G 12H

TWO STAGE HYDROCRACKER U-O-S BLOCK SECTION BLOCK: MIXER12 MODEL: MIXER (CONTINUEO)

***

HASS AND ENERGY BALANCE ***

IN OUT 1.42668 41.3410 .426899E+08 *** INPUT DATA """ 1.42668 41.3410 .426909E+08 RELATIVE DIFF_ .OOOOOOE+OO -.515620E-15 -.256989E-04 30 0.00010000 OUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES

BLOCK: HIXER13 MODEL: MIXER

INLET STREAMS: OUTLET STREAM: PROPERTY OPTION SET:

TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPYCIIATT

""*

15 11A

11B

SYSOP4 PENG-ROBINSON EQUATION OF STATE MASS AND ENERGY BALANCE """

IN OUT .541539 51.0000 .362901E+08 *** INPUT DATA *** .541539 51.0000 .362905E+08 RELATIVE OIFF. .OOOOOOE+OO -.278644E-15 -.103980E-04 30 0.00010000 OUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES

BLOCK: MIXER14 MODEL: MIXER INLET STREAMS:

OUTLET STREAM: PROPERTY OPTION SET:

11C

110 SYSOP4

16

PENG-ROBINSON EQUATION OF STATE

"

MASS ANO ENERGY BALANCE ***

TOTAL BALANCE MOLE(KMOL/SEC) MASS(KG/SEC ) ENTHALPY(IIATT IN OUT .711221 51.5000 .394558E+08 .711221 51.5000 .394571 E+08 RELATIVE DI FF. .OOOOOOE+OO • 137969E -15 -.317264E-04

(27)

U-O-S BLOCK SECTION

BLOCK: MIXER14 MODEL: MIXER (CONTINUED)

*** INPUT DATA ***

TYO PHASE FLASH

CONVERGENCE TOLERANCE 30 0.00010000

INLET STREAMS: 10 3

OUTLET STREAM:

TOTAL BALANCE

ENTHALPY(YATT ***

TYO PHASE FLASH

MASS AND ENERGY BALANCE •• *

IN OUT .450822 38.7000 . 256984E+08 *** INPUT DATA **. .450822 38.7000 . 256982E+08

OUT LET PRESSURE: MINIMUM OF INLET STREAM PRESSURES

BLOCK: MIXER3 MODEL: MIXER

INLET STREAMS: 42 44 OUTLET STREAM: RELATIVE DIFF. .OOOOOOE+OO .183603E-15 .801752E-05 30 0.00010000

TOTAL BALANCE

T~O PHASE FLASH

MASS ANO ENERGY BALANCE ***

IN CUT .453541 87.7812 -.151602E+08 *** INPUT DATA *** .453541 87.7812 -.151602E+08

OUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES

CRACK3.REP 13/08/1993 RELATIVE OIFF. .157016E-06 -.184541E-06 .212478E-06 30 0.00010000

U-O-S BLOCK SECTION

BLOCK: MIXER7 MODEL: MIXER

INLET STREAMS: 8B 34

CUTLET STREAM:

MASS(KG/SEC )

TYO PHASE FLASH

MASS AND ENERGY BALANCE **.

IN OUT 1.52966 3.34104 653603. ••• INPUT DATA ••• 1.52966 3.34104 653580.

CUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES BLOCK: MIXER8 MODEL: MIXER

INLET STREAMS: 18 CUTLET STREAM: RELATIVE DIFF. .OOOOOOE+OO .OOOOOOE+OO .349304E-04 30 0.00010000

12A 12B

MASS(KG/SEC )

ENTHALPY(YATT

•••

TYO PHASE FLASH

MASS AND ENERGY BALANCE **.

IN CUT .694777 39.3610 . 297678E+08 ••• INPUT OATA *** .694777 39.3610 . 297684E+08

CUTLET PRESSURE: MINIMUM OF INLET STREAM PRESSURES BLOCK: MIXER9 MODEL: MIXER

INLET STREAMS: 19

CUT LET STREAM:

RELATIVE DIFF. .OOOOOOE+OO .361039E-15 -.182611E-04 30 0.00010000

12C

12D