Coker A.K. Fortran Programs for Chemical Process Design, Analysis, and Simulation
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WRITE (i, 210)I, N(I), DP(I)
FORMAT (12X, I2, 16X, F8.4, 20X, F8.4)
END DO
WRITE (I, 220)DPT
FORMAT(IH ,76(IH-),/,6X,'TOTAL DEW POINT:', T59, F8.4)
IF (DPT .GE. 1.0) THEN
GO TO I0
ELSE
WRITE (i, 230)
FORMAT(/,6X,'LOWER THE DEW-POINT TEMPERATURE: oF')
ENDIF
GO TO 20
WRITE (I, 240)
FORMAT(/,6X,'RAISE THE DEW-POINT TEMPERATURE: oF')
FORM FEED THE PRINTING PAPER TO THE TOP OF THE NEXT PAGE.
WRITE (I, *) CHAR(12)
RETURN
END
THIS PROGRAM CALCULATES THE BUBBLE-POINT
*****************************************************************
SUBROUTINE BUBBLE
COMMON/DATA/BP,DP,J,K,N
REAL N(20), K(20), DP(20), BP(20)
BPT=0.0
DO I = i, J
BP(I) =N(I)*K(I)
BPT=BPT+N(I)*K(I)
END DO
WRITE (I, 250)
FORMAT (/,6X, 'NUMBER OF COMPONENTS', 6X, 'MOLE FRACTION',I6X,
"Y=KX',/IH ,76(IH-))
DO I =i ,J
WRITE (i, 260) I, N(I), BP(I)
FORMAT (12X, I2, 16X, F8.4, 20X, F8.4)
END DO
WRITE (i, 270)BPT
FORMAT(IH ,76(IH-),/,6X,'TOTAL BUBBLE POINT:', T59, F8.4)
IF (BPT .GE. 1.0) THEN
GO TO 30
ELSE
WRITE (i, 280)
FORMAT(/,6X,'RAISE THE BUBBLE POINT TEMPERATURE: oF')
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ENDIF
GO TO 35
WRITE (i, 290)
FORMAT(/,6X,'LOWER THE BUBBLE POINT TEMPERATURE: oF')
FORM FEED THE PRINTING PAPER TO THE TOP OF THE NEXT PAGE.
WRITE (i, *) CHAR(12)
RETURN
END
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PROGRAM PROG72
EQUILIBRIUM FLASH CALCULATIONS
THE PROGRAM USES THE ITERATIVE CONVERGENCE METHOD SUGGESTED BY
I.H. OLIVER AND LATER MODIFIED BY S.T. KOSTECKE TO CALCULATE
FLASH VAPORIZATION CONTAINING UP TO 15 COMPONENTS OF
MULTICOMPONENT MIXTURES OF OIL, GAS AND CHEMICAL PROCESSES.
THIS PROGRAM FURTHER CHECKS THE FEED COMPOSITION AT THE
CONDITIONS GIVEN TO DETERMINE WHETHER THE FEED IS ALL VAPOR
OR ALL LIQUID. THIS PROGRAM IS BASED ON THE WELL-KNOWN AND
WIDELY USED VAPORIZATION EQUILIBRIUM RELATIONSHIPS THAT
APPEAR IN HANDBOOKS BY THE NATURAL GAS PROCESSORS SUPPILIERS
ASSOCIATIONS AND IN OTHER LITERATURE.
**************************************************************
Mi =
Ki =
R "-
R1 =
L =
V =
Ni =
Li =
Vi =
X =
y =
TOTAL MOLES OF COMPONENT i IN THE FEED STREAM
EQUILIBRIUM FLASH CONSTANT FOR EACH COMPONENT i
IN THE FEED STREAM
L/V RATIO
NEW L/V RATIO FOR EACH ITERATIVE CALCULATION
TOTAL MOLES OF LIQUID AT EQUILIBRIUM CONDITIONS
TOTAL MOLES OF VAPOR AT EQUILIBRIUM CONDITIONS
MOLES FRACTION OF COMPONENT i IN THE FEED STREAM
TOTAL MOLES OF COMPONENT i IN THE LIQUID PHASE
TOTAL MOLES OF COMPONENT i IN THE VAPOR PHASE
MOLE FRACTION OF FEED IN THE LIQUID PHASE AT EQUILIBRIUM
MOLE FRACTION OF FEED IN THE VAPOR PHASE AT EQUILIBRIUM
E,F = CONSTANTS USED BY KOSTECKS
***************************************************************
DIMENSION C(15), V(15), XI(15), YI(15)
REAL K(15), LI, L(15), M(15), N(15)
COMMON/DATA1/ NUM, T, P, M, K
COMMON/DATA2/ ADD1, ADD2, ADD3
OPEN (UNIT = 3, FILE='DATA72.DAT ' , STATUS='OLD', ERR=I8)
OPEN (UNIT = i, FILE='PRN')
READ FLASH TEMPERATURE, oF = T
READ FLASH PRESSURE, psia = P
READ NUMBER OF COMPONENTS = NUM
READ FEED AND EQUILIBRIUM CONSTANT OF EACH COMPONENT = M, K
READ (3, *, ERR=I9) T
READ (3, *, ERR=I9) P
READ (3, *, ERR=I9) NUM
DO I = I, NUM
READ (3, *, ERR=I9) M(I), K(I)
END DO
GO TO i0
WRITE (*, i00)
FORMAT (5X, 'DATA FILE DOES NOT EXIST')
GO TO 999
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i0
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45
60
65
WRITE (*, ii0)
FORMAT (5X, 'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
WRITE(I, 120)
FORMAT(//,20X,'MULTICOMPONENT EQUILIBRIUM FLASH CALCULATIONS')
SUM=0.0
DO I = i, NUM
SUM = SUM + M(I)
END DO
CALCULATE MOLE FRACTION OF COMPONENT IN THE FEED STREAM
DO I = I, NUM
N(I)=M(I)/SUM
END DO
TOTAL=0.O
DO I = i, NUM
TOTAL = TOTAL + N(I)
END DO
CHECK WHETHER THE FEED IS ALL LIQUID OR VAPOR
SUM1=0.0
DO Ii = i, NUM
SUM1 = SUM1 + N(II)*K(II)
END DO
IF ( SUM1 .GT. 1.0) THEN
GO TO 45
ELSE
GO TO 900
ENDIF
SUM2 = 0.0
DO I2 = i, NUM
SUM2 = SUM2+N(I2)/K(I2)
END DO
IF(SUM2 .GT. 1.0) THEN
GO TO 60
ELSE
GO TO i000
ENDIF
GUESS R=L/V
R=I.
0
SUM3=0.0
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90
DO I3
= i,
NUM
C(I3)=(M(I3)*(K(I3)-I.0)*(R+I.0) )/(K(I3)+R)
END DO
CALCULATE E AND F CONSTANTS USED BY KOSTECKE.
E = 0.0
F = 0.0
DO I4 = 1, NUM
E = E+C(I4)
F = F+(C(I4)**2/M(I4) )
END DO
CALCULATE RI, THE NEW L/V RATIO
RI=ABS((F*R-E*(R+I.0))/(F+E*(R+I.0)))
IF (ABS(E) .LT. 0.001) THEN
GO TO 90
ELSE
R=RI
GO TO 65
ENDIF
L1 = 0.0
V1 = 0.0
DO I5 = I, NUM
L(I5) = (M(I5)*RI)/(K(I5)+RI)
V(I5) = M(I5)-L(I5)
L1 = L1 + L(I5)
vl = vl + v(I5)
END DO
R2=LI/VI
CALCULATE X: MOLE FRACTION OF FEED IN THE LIQUID PHASE
AT EQUILIBRIUM, AND Y: MOLE FRACTION OF FEED IN THE VAPOR
PHASE AT EQUILIBRIUM.
VALI=0.0
VAL2=0.0
VAL3=0.0
DO I6 = I, NUM
VALI = VALI+L(I6)
VAL2 = VAL2+M(I6)
VAL3 = VAL3+V(I6)
END DO
CALCULATE THE MOLE FRACTIONS IN THE LIQUID AND VAPOR PHASES.
DO I = 1, NUM
X1 ( I ) =L( I )/VALI
Y 1 ( I ) =V ( I )/VAL 3
END DO
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i000
400
999
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CALCULATE THE TOTAL MOLE FRACTIONS OF THE FEED, LIQUID AND
VAPOR PHASES
ADD1 = 0.0
ADD2 = 0.0
ADD3 = 0.0
DO I = I, NUM
ADD1 = ADDI+XI(I)
ADD2 = ADD2+N(I)
ADD3 = ADD3+YI(I)
END DO
PRINT THE RESULTS ON THE SCREEN
CALL OUTPUT(N, L, XI, V, Yl, VALI, VAL2, VAL3)
PRINT THE RESULTS ONTO THE PRINTER
CALL PAPER (N, L, Xl, V, Yl, VALI, VAL2, VAL3)
GO TO 999
WRITE(*,300)
FORMAT(3X,'THE FEED COMPOSITION IS ALL LIQUID')
GO TO 999
WRITE(*,400)
FORMAT(3X,'THE FEED COMPOSITION IS ALL VAPOR')
CLOSE (UNIT=3, STATUS='KEEP')
CLOSE (UNIT=l)
STOP
END
***************************************************************
THIS PROGRAM OUTPUTS THE RESULTS ON THE SCREEN
****************************************************************
SUBROUTINE OUTPUT (N, L, Xl, V, u VALI, VAL2, VAL3)
DIMENSION Xl(15), YI(15), V(15)
REAL K(15), M(15), N(15), L(15)
COMMON/DATA1/ NUM, T, P, M, K
COMMON~DATA2~
ADD1, ADD2, ADD3
WRITE(*, 130)
FORMAT(2X,'MULTICOMPONENT EQUILIBRIUM FLASH CALCULATION AT '\)
WRITE(*, 140) T, P
FORMAT(F6. I,IX,'DEG . F' , IX , 'AND' , IX,F6 . I,IX,'PSIA')
WRITE(*, 150)
FORMAT(79(IH*))
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WRITE(*, 160)
FORMAT(/,IX,'COMPONENT',IX,'K-VALUE',6X,'FEED',I6X,'LIQUID ',\)
WRITE(*, 170)
FORMAT(15X,'VAPOR')
WRITE(*, 180)
FORMAT(1X,'NUMBER',12X,'Mols/h.',2X,'Mol. frac.',2X,'Mols/h.',\)
WRITE(*, 190)
FORMAT(2X,'Mol.frac.',2X,'Mols/h.',2X,'Mol.frac.')
WRITE(*, 200)
FORMAT(78(IH-))
DO I = I, NUM
WRITE(*, 210) I, K(I), M(I), N(I), L(I), XI(I), V(I)
FORMAT( IX,I2,5X, F5.3,2X, F9.3,2X, F8.3,3X, F9.3,2X, F8.3,2X, F9.3\)
WRITE(*,
220)
u
FORMAT(2X,F8.3)
END DO
WRITE(*, 230)
FORMAT(78(IH-))
WRITE(*, 240) VAL2, ADD2, VALI, ADD1
FORMAT(2X,'TOTALS',TX,F9.3,5X,F5.3,3X,F9.3,5X,F5.3,\)
WRITE(*, 250) VAL3, ADD3
FORMAT(2X,F9.3,5X,F5.3)
WRITE(*, 260)
FORMAT (78(IH-))
RETURN
END
THIS PROGRAM PRINTS THE RESULTS ONTO THE PRINTER
***************************************************************
SUBROUTINE PAPER (N, L, X1, V, Y1, VAL1, VAL2, VAL3)
DIMENSION V(15), XI(15), u
REAL K(15), L(15), M(15), N(15)
COMMON/DATA1/NUM, T, P, M, K
COMMON/DATA2/ADD1, ADD2, ADD3
WRITE (1, 270)
270 FORMAT (/,2X,'MULTICOMPONENT EQUILIBRIUM FLASH CALCULATION AT ',\)
WRITE (1, 280) T, P
280 FORMAT (F6.1, 1X, 'DEG. F', 1X, 'AND', 1X, F6.1, 1X, 'psia')
WRITE (i, 290)
290 FORMAT (80(IH*))
553
WRITE (i, 300)
300 FORMAT (/, IX,'COMPONENT', IX,'K-VALUE',6X,'FEED',I6X,'LIQUID ',\)
WRITE (i, 310)
310 FORMAT (15X, 'VAPOR')
WRITE (i, 320)
320 FORMAT (IX, 'NUMBER',I2X,'Mols/h.',2X,'Mol. frac.',2X,'Mols/h.',\)
WRITE (i, 330)
330 FORMAT (2X,'Mol. frac.', 2X, 'Mols/h.', 2X,'Mol. frac.')
WRITE (I, 340)
340 FORMAT (80(IH-))
DO I = i, NUM
WRITE (i, 350) I, K(I), M(I), N(I), L(I), XI(I), V(I)
350 FORMAT (IX,I2,5X,F5.3,2X,F9.3,2X,FS.3,3X,F9.3,2X,F8.3,2X,F9.3,\)
WRITE (i, 360) YI(I)
360 FORMAT (2X,F8.3)
END DO
WRITE (I, 370)
370 FORMAT (80(IH-))
WRITE (I, 38.0) VAL2, ADD2, VALI, ADD1
380 FORMAT (2X,'TOTALS', 7X, F9.3, 5X, F5.3, 3X, F9.3, 5X, F5.3,\)
WRITE (i, 390) VAL3, ADD3
390 FORMAT (2X, F9.3, 5X, F5.3)
WRITE (I, 400)
400 FORMAT (80(IH-))
C FORM FEED THE PRINTING PAPER ON TOP OF THE NEXT PAGE.
WRITE (i, *) CHAR(12)
RETURN
END
554
PROGRAM PROG73
TOWER SIZING FOR VALVE TRAYS.
THE PROGRAM EMPLOYS THE NUTTER METHOD FOR CALCULATING
TOWER DIAMETER WHERE VALVE-TYPE TRAYS ARE USED.
TOWER SIZING GRAPHS AND CURVES IN NUTTER'S FLOAT VALVE
DESIGN HAVE BEEN FITTED TO A SERIES OF EQUATIONS AND ARE
USED IN THIS PROGRAM.
***************************************************************
RD = DENSITY RADICAL
DENV = VAPOR DENSITY, ib/ft.^3
DENL = LIQUID DENSITY, ib/ft.^3
SURT = SURFACE TENSION, dyne/cm.
v = VELOCITY AT ZERO LIQUID LOAD, ft./sec.
FT = TRAY SPACING FACTOR
WV = VAPOR FLOW RATE, ib/hr.
VCFS = VOLUMETRIC VAPOR FLOW RATE, ft.^3/sec.
WL = LIQUID FLOW RATE, ib/hr.
LCFS = VOLUMETRIC LIQUID FLOW RATE, ft.^3/sec.
AB = BUBBLING AREA, ft.^2.
FF = FOAM FACTOR
ADC = DOWNCOMER AREA, ft.^2.
REST = DOWNCOMER RESIDENCE TIME, sec.
TS = TRAY SPACING, inch.
TSF = SAFETY FACTOR
AT = TOWER AREA, ft^2
D = TOWER DIAMETER, ft.
***************************************************************
REAL K, M, LCFS
COMMON PI
COMMON/MULTI/ X, SF, RD, V, VRD
COMMON/MULT2/ AB, ADC, AT, DIA, RDCA
COMMON/MULT3/
WV, WL, DENL, DENV, FF, REST, TS, SURT
COMMON/MULT4/ LCFS, VCFS
OPEN (UNIT=3,FILE='DATA73.DAT',STATUS='OLD',ERR=I8)
OPEN (UNIT=I,FILE='PRN')
READ THE VAPOR FLOW RATE, WV: ib/hr.
READ THE LIQUID FOW RATE, WL: Ib/hr.
READ THE LIQUID DENSITY, DENL: Ib/ft^3.
READ THE VAPOR DENSITY, DENL: Ib/ft^3.
READ THE FOAM FACTOR, FF:
READ THE DOWNCOMER RESIDENCE TIME, REST: sec.
READ THE TRAY SPACING, TS:
READ THE SURFACE TENSTION, SURT: dyne/cm.
READ(3, *
READ(3, *
READ(3, *
, ERR=I9) WV, WL, DENL
, ERR=I9) DENV, FF, REST
, ERR=I9) TS, SURT
GO TO 20
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24
WRITE (*, 21)
FORMAT(3X,'DATA FILE DOES NOT EXIST')
GO TO 999
WRITE (*, 22)
FORMAT(3X,'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
CONSTANTS FOR VELOCITY AT ZERO LIQUID LOAD, ft/sec.
(W.W. BLACKWELL, Chemical Process Design On A Programmable
Calculator, Mc. Graw-Hill, 1984).
PI = 3.1415927
A = 0.22982
B = 0.44605
C = 0.03452
D = 0.00415
E = 0.00017
K = 0.91146
M = -0.03821
CALCULATE THE RATIO OF SURFACE TENSION TO THE VAPOR DENSITY, X
X=SURT/DENV
CALCULATE THE SAFETY FACTOR.
SF=K* ( X ) * *M
CALCULATE THE DENSITY RADICAL.
RD=SQRT ( DENV/( DENL-DENV ) )
V IS VALID FOR 0.I < X < 3000.
CALCULATE THE VELOCITY AT ZERO LIQUID LOAD, ft/sec.
VALI=A+B*ALOG (X) -C* (ALOG (X) ) ** 2+D* (ALOG ( X ) ) **3-E* (ALOG (X) ) **4
V=EXP ( VALI )
VRD=V*RD
IF (VRD .GE. 0.5) THEN
GO TO 23
ELSE
ENDIF
GO TO 24
VRD = 0.5
CHECK THE TRAY SPACING, TS.
IF (TS .EQ. 12.0 ) THEN
GO TO 33
ELSEIF (TS .EQ. 18.0) THEN
556