Coker A.K. Fortran Programs for Chemical Process Design, Analysis, and Simulation
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Equipment Sizing
Table 4-8
Input Data and Computer Output for Cyclone Design
297
DATA44.DAT
26.333 8.552 6.333 2.533
4.5 1.896 3.448 3.792
516.7 62.43 0.075 0.0000128
ii0.0 0.00003281
CYCLONE DESIGN
CYCLONE OVERALL HEIGHT, ft:
CYCLONE CYLINDRICAL HEIGHT, ft.:
CYCLONE DIAMETER, ft.:
CYCLONE DUST-OUTLET DIAMETER, ft:
CYCLONE GAS INLET LENGTH, ft:
CYCLONE GAS INLET WIDTH, ft:
CYCLONE GAS OUTLET LENGTH, ft:
CYCLONE GAS OUTLET DIAMETR, ft:
GAS RATE, ft^3/s.:
PARTICLE DENSITY, ib/ft^3:
GAS DENSITY, ib/ft^3:
GAS VISCOSITY, Ib/ft.s.:
GAS TEMPERATURE, oF:
PARTICLE SIZE (EQUIVALENT DIA.),ft.:
VORTEX EXPONENT:
RELAXATION TIME, s:
INLET FLUID VELOCITY, ft/s.:
SALTATION VELOCITY, ft/s.:
CYCLONE CONFIGURATION FACTOR:
CYCLONE PRESSURE DROP, in H20:
RATIO OF THE INLET TO THE SALTATION VELOCITIES:
CYCLONE EFFICIENCY, %:
EFFECTIVE NUMBER OF TURNS:
CRITICAL PARTICLE DIAMETER, ft.:
CRITICAL PARTICLE DIAMETER, microns:
RATIO OF PARTICLE DIA. TO CRITICAL DIA.:
26.333
8.552
6.333
2.533
4.500
1.896
3.448
3.792
516.70
62.430
.075
.128000E-04
ii0.000
.328100E-04
.7276
.291691E-03
60.560
22.108
89.728
7.834
2.739
63.305
3.71
.643700E-04
.196200E+02
.51
Table 4-9
Dryer Parameters
Flow = 65 MM std ft3/day
P = 700 psig
T = 80~
Z = 0.9228
H20 Cont = 47 lb/MM std ft 3
S = 15,500 lb/in 2
E= 1.0
Cycle = 12h
Desiccant H20 cap = 8%
Desiccant density = 50
lb/ft 3
Desiccant bed length = 15ft
Heater outlet = 500~
MW= 18
H ~ = 490 B tu/lb
H 2 = 225 Btu/lb
h = 2.0ft
298 Fortran Programs for Chemical Process Design
From Figure 4-10,
Superficial gas velocity = 35 ft/min
Desiccant bed length = 15.0 ft
System pressure = 700 psig
The clean bed AP using Equation 4-79 is
AP - 0.87 ft H20 ( 0.4335psi
ftbed ~, ftH20
) /18) ~
(15.0 ft bed) -~
= 3.68psi
Table 4-10
Input Data and Computer Output for Gas Dryer Design
DATA45.DAT
65.0 700.0 80.0
0.9228 12.0 47.0
15500.0 1.0 8.0
50.0 15.0 500.0
18.0 490.0 225.0
GAS DRYER DESIGN
******************************************************************************
GAS FLOW RATE, 10^6 std. ft^3/day:
DRYER OPERATING PRESSURE,
psig.:
GAS FLOWING TEMPERATURE, oF:
GAS COMPRESSIBILITY FACTOR:
DRYING CYCLE,
hr.:
WATER CONTENT OF GAS, ib/10^6 std.ft^3:
ALLOWABLE STRESS,
psi:
JOINT EFFICIENCY:
USEFUL DESIGN CAPACITY OF DESICCANT, (%):
DESICCANT DENSITY, ib/ftA3:
HEATER OUTLET TEMPERATURE,
oF:
MOLECULAR WEIGHT OF REGENERATION GAS:
ENTHALPY OF GAS BEFORE REGENERATION HEATER, Btu/Ib:
ENTHALPY OF GAS AFTER REGENERATION HEATER, Btu/Ib:
TOTAL WATER ADSORBED, ib/h.:
DESICCANT VOLUME, ftA3.:
CALCULATED CROSS-SECTIONAL AREA, ftA2.:
BED DIAMETER, ft.:
BED RADIUS, ft.:
BED LENGTH, ft.:
ACTUAL GAS FLOW RATE, ft^3/min.:
SUPERFICIAL GAS VELOCITY, ft./min.:
DRYER SHELL THICKNESS, in.:
VESSEL WEIGHT, lb.:
DESICCANT WEIGHT, lb.:
TEMPERATURE OF DESICCANT BED, oF:
TOTAL HEAT REQUIRED TO REGENERATE DRYER, Btu:
LOSS FACTOR:
HEAT ADDED TO REGENERATION GAS:
TOTAL REGENERATION GAS REQUIREMENT, ib:
STANDARD CUBIC FEET OF REGENERATION GAS, std.ft^3:
MOMENTUM:
65.000
700.000
80.0
.9228
12.0
47.
15500.0
1.0
8.0
50.0
500.0
18.0
490.0
225.0
1527.500
381.8750
25.4583
5.6934
34.1603
15.00
889.697
34.947
1.5857
24767.
19094.
487.500
.555954E+07
2.1282
.I18320E+08
.446490E+05
.942590E+06
.305838E+05
Equipment Sizing 299
Fouled AP- 3.68 x 1.6
= 5.89 psi
The actual regeneration flow rate (lb/h) will depend upon the length of
the heating cycle used.
References
1. Watkins, R. N., "Sizing Separators and Accumulators," Hydrocar-
bon Process, Vol. 46, No. 11, Nov. 1967, pp. 253-256.
2. Backwell, W. W., "Chemical Process Design on a Programmable
Calculator," McGraw-Hill, Inc., New York, 1984.
3. Gerunda, A., "How to Size Liquid-Vapor Separators," Chem. Eng.,
May 4, 1981, pp. 81-84.
4. Kowal, G., "Quick Calculations for Holdups In Horizontal Tanks,"
Chem. Eng., June 11, 1973, pp. 130-132.
5. Evans, E L., Equipment Design Handbook for Refineries and Chemi-
cal Plants, Vol. 2, Gulf Publishing Co., Houston, 1980.
6. Kelsall, M. A., A Study of the Motion of Solids Particles in a Hydraulic
Cyclone, Trans. Inst. Chem. Engrs., Vol. 30, 1952, pp. 87-108.
7. Coker, A. K., and G. V. Jeffreys, "Flow Patterns and Residence Time
Distribution in Nozzle-Type Reactors," Inst. Chem. Symp. Ser. No.
108, Fluid Mixing III, 1987, p. 105.
8. Coker, A. K., "A Study of Fast Reactions in Nozzle-Type Reac-
tors," Ph.D. Thesis, Aston University, U.K., 1985.
9. Coker, A. K., G. V., Jeffreys, and C. J. Mumford, "Mechanisms of
Nozzle-Type Reactor Operations with Gas Removal," Scientific
Research, Vol. 49, 1992, pp. 67-81.
10. Stairmand, C. J., "Design and Performance of Cyclone Separators,"
Trans. Inst. Vol. 29, 1951, p. 356.
11. Strauss, N., Chapter 6, Industrial Gas Cleaning, Pergamon Press,
N.Y., 1966.
12. Koch, W.H. and Licht, W. L., "New Design Approach Boosts
Cyclone Efficiency," Chem. Eng., Nov. 1977, pp. 80-88.
13. Zenz, E A., Ind & Eng. Chem. Fund., Vol. 3, 1964, p. 65.
14. Kalen, B. and Zenz, E A., AIChE. Symp. Ser. Vol. 70, No. 137,
1974, p. 388.
15. Lieberman, N. R, Troubleshooting Process Operations, 2nd. Ed.,
PennWell Books, Oklahoma, 1985.
16. Walas, S. M., Chemical Process Equipment~Selection and Design,
Butterworths Series in Chemical Engineering, 1988.
300
Fortran Programs for Chemical Process Design
17. Engineering Data Book,
10th Ed., Vol. 2, Gas Processors Suppliers
Association, Tulsa, Oklahoma, 1987.
18. Wunder, J. W., "How to Design a Natural Gas Drier,"
Oil Gas J.,
Aug. 6, 1962, pp. 137-148.
HL =
SFac(SF)=
KV =
VM =
WL =
WV =
DENL =
DENV =
QV =
D =
A =
AV =
QL =
T =
KH =
AT =
L =
AL =
PROGRAM PROG41
THIS PROGRAM USES THE WELL-KNOWN SOUDERS AND BROWN CORRELATION
COUPLED WITH LIQUID SURGE CAPACITY TO SIZE LIQUID-VAPOR SEPARATORS.
THE PROGRAM SIZES BOTH VERTICAL AND HORIZONTAL SEPARATORS
LIQUID HEIGHT, ft.
SEPARATION FACTOR
VAPOR VELOCITY FACTOR FOR VERTICAL SEPARATORS
MAXIMUM VAPOR VELOCITY, ft/s
LIQUID FLOW RATE, ib/hr.
VAPOR FLOW RATE, ib/hr.
LIQUID DENSITY, ib/ft^3.
VAPOR DENSITY, ib/ft^3
VAPOR VOLUMETRIC FLOW, ft^3/s
VESSEL DIAMETER, ft
CROSS-SECTIONAL AREA OF VERTICAL SEPARATOR, ft^2
MINIMUM CROSS-SECTIONAL AREA OF VERTICAL SEPARATOR, ft^2
LIQUID VOLUMETRIC FLOW, ft^3/s
LIQUID SURGE TIME, min.
VAPOR VELOCITY FACTOR FOR HORIZONTAL SEPARATORS
TOTAL CROSS-SECTIONAL AREA OF HORIZONTAL VESSEL, ft^2
HORIZONTAL VESSEL LENGTH, ft
CRDSS-SECTIONAL AREA OF HORIZONTAL VESSEL OCCUPIED BY
LIQUID PHASE, ft^2
X = in(S.Fac)
**********************************************************************
REAL KH, KVl, L
COMMON B, D, E, F, G, PI
COMMON/DATA1/ WLI, WVI, DENLI, DENVI, T1
COMMON/DATA2/ SFI, KVl, VMAXI, D1
COMMON/DATA3/ UMAX, UMIN, QLI, QVl, V, HL
COMMON~DATA4~
WL2, WV2, DENL2, DENV2, RATIO
COMMON~DATA5~
SF2, KH, QL2, QV2, VMAX2, D2, L, VESVOL, T2, CALT2
OPEN (UNIT=3, FILE='DATA41.DAT', STATUS='OLD', ERR=I8)
OPEN (UNIT=l, FILE='PRN ' )
PI = 3.1415927
CONSTANTS FOR VAPOR VELOCITY FACTOR
B = -1.877478
D = -0.814580
E = -0.187074
F = -0.014523
G = -0.001015
READ (3, *, ERR=I9) I
GO TO (ii, 22),I
READ LIQUID FLOW RATE, WLI: ib/hr.
301
II
22
18
20
19
21
C
33
C
C
44
C
999
C
C
READ VAPOR FLOW RATE, WVI: ib/hr.
READ LIQUID DENSITY, DENLI: ib/ft^3.
READ VAPOR DENSITY, DENVI: ib/ft^3.
READ LIQUID SURGE TIME, TI: min.
READ (3, *, ERR=I9) WLI, WVI
READ (3, *, ERR=I9) DENLI, DENVI
READ (3, *, ERR=I9) T1
GO TO 33
READ LIQUID FLOW RATE, WL2: Ib/hr.
READ VAPOR FLOW RATE, WV2: ib/hr.
READ LIQUID DENSITY, DENL2: ib/ft^3.
READ VAPOR DENSITY, DENV2: ib/ft^3.
READ LIQUID SURGE TIME, T2: min.
READ LENGTH-TO-DIAMETER RATIO, RATIO.
READ (3, *, ERR=I9) WL2, WV2
READ (3, *, ERR=I9) DENL2, DENV2, T2
READ (3, *, ERR=I9) RATIO
GO TO 44
WRITE (*, 20)
FORMAT (6X, 'DATA FILE DOES NOT EXIST')
GO TO 999
WRITE (*, 21)
FORMAT (6X, 'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
COMPUTE THE SIZING OF THE VERTICAL SEPARATOR
CALL VERT
OUTPUT THE RESULTS OF THE VERTICAL SEPARATOR
CALL OUTV
GO TO 5
COMPUTE THE SIZING OF THE HORIZONTAL SEPARATOR
CALL HORIZ
OUTPUT THE RESULTS OF THE HORIZONTAL SEPARATOR
CALL OUTH
GO TO 999
CLOSE (3, STATUS='KEEP')
CLOSE (i)
STOP
END
***************************************************************
THIS PROGRAM SIZES VERTICAL LIQUID-VAPOR SEPARATORS
302
***************************************************************
SUBROUTINE VERT
REAL KVl
COMMON B, D, E, F, G, PI
COMMON~DATA1~
WLI, WVl, DENLI, DENVl, T1
COMMON/DATA2/ SFI, KVI, VMAXI, D1
COMMON/DATA3/ UMAX, UMIN, QLI, QVI, V, HL
CALCULATE THE SEPARATION FACTOR
SFI = (WLI/WVI)*SQRT(DENVl/DENLI)
X1 = ALOG(SFI)
VALI = B+(D*XI)+(E*(XI**2))+(F*(XI**3))+(G*(XI**4))
CALCULATE THE VAPOR VELOCITY FACTOR, ft./s.
KVI = EXP(VALI)
CALCULATE THE MAXIMUM VAPOR VELOCITY, ft./s.
VMAXI
=
KVI*SQRT((DENLI-DENVI)/DENVI)
CALCULATE THE VOLUMETRIC RATE, ftA3/sec.
QVI = WVl/(DENVI*3600.0)
AVI = QVI/VMAXI
CALCULATE THE DIAMETER OF THE VESSEL, ft.
D1 = SQRT((4.0*AVI)/PI)
AREA = (PI*DI**2)/4.0
CALCULATE THE VAPOR-LIQUID INLET NOZZLE VELOCITIES.
DENM = (WLI+WVl)/((WLI/DENLI)+(WVI/DENVI))
UMAX = IO0.O/(DENM**0.5)
UMIN = 60.O/(DENM**0.5)
CALCULATE THE LIQUID VOLUMETRIC RATE, ft^3/sec.
QLI = WLI/(DENLI*3600.)
CALCULATE THE REQUIRED VESSEL VOLUME, ft^3.
V = (QLI*TI*60~
CALCULATE THE LIQUID HEIGHT, ft.
HL = V/AREA
RETURN
END
***************************************************************
THIS PROGRAM SIZES HORIZONTAL LIQUID-VAPOR SEPARATOR
***************************************************************
SUBROUTINE HORIZ
REAL L, KH, KV2
COMMON B, D, E, F, G, PI
COMMON/DATA4/ WL2, WV2, DENL2, DENV2, RATIO
COMMON/DATA5/ SF2, KH, QL2, QV2, VMAX2, D2, L, VESVOL, T2, CALT2
303
i00
CALCULATE THE VAPOR-LIQUID SEPARATION FACTOR
SF2 = (WL2/WV2)*SQRT(DENV2/DENL2)
X2 = ALOG(SF2)
VAL2 = B+(D*X2)+(E*(X2**2))+(F*(X2**3))+(G*(X2**4))
KV2 = EXP(VAL2)
CALCULATE THE VAPOR VELOCITY FACTOR FOR HORIZONTAL SEPARATOR
KH = 1.25"KV2
VMAX2 = KH*SQRT((DENL2-DENV2)/DENV2)
CALCULATE THE LIQUID VOLUMETRIC RATE, ft^3/sec.
QL2 = WL2/(DENL2*3600.0)
CALCULATE THE VAPOR VOLUMETRIC RATE, ft^3/sec.
QV2 = WV2/(DENV2*3600.0)
CALCULATE THE VAPOR FLOW AREA, ft^2.
AV2 = QV2/VMAX2
CALCULATE THE TOTAL CROSS-SECTIONAL AREA
OF HORIZONTAL VESSEL, ft^2.
AT = AV2/0.2
CALCULATE THE DIAMETER, ft.
D2 = SQRT((4.0*AT)/PI)
ASSUMING THE LENGTH TO DIAMETER RATIO = 3
THE LENGTH TO DIAMETER RATIO, (i.e. RATIO=L/D=3)
L = RATIO*D2
THE SEPARATOR VAPOR AREA IS ASSUMED TO OCCUPY 20% OF THE TOTAL
CROSS-SECTIONAL AREA. THEREFORE THE LIQUID AREA WILL OCCUPY 80% OF
THE TOTAL CROSS-SECTIONAL AREA.
CALCULATE THE FILL LIQUID VOLUME, ft^3.
AL = 0.8*AT
CALCULATE THE VESSEL VOLUME, ft^3.
VESVOL = AT*L
CALCULATE THE LIQUID SURGE TIME, min.
CALT2 = (AL*L*DENL2*60.)/WL2
RETURN
END
***********************************************************
THIS PROGRAM PRINTS THE RESULTS OF THE VERTICAL SEPARATOR
***********************************************************
SUBROUTINE OUTV
REAL KVl
COMMON~DATA1~
WLI, WVl, DENLI, DENVI, T1
COMMON/DATA2/ SFI, KVl, VMAXl, D1
COMMON/DATA3/ UMAX, QLI, QVI, UMIN, V, HL
WRITE (i, i00)
FORMAT (///,25X, 'VERTICAL SEPARATOR SIZING',/,78(IH*))
304
ii0
120
130
140
150
160
170
180
190
WRITE (i, ii0) WLI, WVl, DENLI, DENVI, QLI, QVI, T1
FORMAT (SX,'LIQUID FLOWRATE, Ib/hr.:', T60, FI0.0,/,
1 5X,'VAPOR FLOWRATE, ib/hr.:', T60, FI0.0,/,
2 5X,'LIQUID DENSITY, ib/ft^3.: ' , T60, F9.3,/,
3 5X,'VAPOR DENSITY, ib/ft^3.: ' , T60, F9.3,/,
4 5X 'LIQUID VOLUMETRIC RATE ft^3/sec.: ' T60, F9.4,/,
5
5X,'VAPOR VOLUMETRIC RATE, ftA3/sec.: ' , T60, F9.4,/,
6
5X,'LIQUID SURGE TIME, min.:', T60, F6.1)
WRITE (i, 120) SFI, KVI, VMAXI, D1
FORMAT (5X,'SEPARATION FACTOR:', T60, F8.4,/,
1 5X,'VAPOR VELOCITY FACTOR:', T60, F8.3,/,
2
5X,'MAXIMUM VAPOR VELOCITY, ft/s.:',T60, F8.3,/,
3 5X,'VESSEL DIAMETER, ft:', T60,FS.3)
WRITE (i, 130) UMIN, UMAX, V, HL
FORMAT (5X,'MINIMUMVAPOR-LIQUID NOZZLE VELOCITY, ft/s.:', T60,
1 F8.3,/,5X,'MAXIMUM VAPOR-LIQUID NOZZLE VELOCITY, ft/s.:',T60,
2 F8.3,/,5X,'REQUIRED VESSEL VOLUME, ftA3:',T60,FS.3,/,
3 5X,'LIQUID HEIGHT, ft.:',T60, F8.3)
WRITE (I, 140)
FORMAT ( 78 ( IH- ) )
RETURN
END
************************************************************
THIS PROGRAM PRINTS THE RESULTS OF THE HORIZONTAL SEPARATOR
************************************************************
SUBROUTINE OUTH
REAL L, KH
COMMON/DATA4/ WL2, WV2, DENL2, DENV2, RATIO
COMMON/DATAS/ SF2, KH, QL2, QV2, VMAX2, D2, L, VESVOL, T2, CALT2
WRITE(I, 150)
FORMAT(//,25X,'HORIZONTAL SEPARATOR SIZING',/78(IH*))
WRITE (i, 160) WL2, WV2, DENL2, DENV2, QL2, QV2, T2, RATIO
FORMAT (5X,'LIQUID FLOWRATE, Ib/hr.:', T60, FI0.0,/,
1 5X,'VAPOR FLOWRATE, ib/hr.:', T60, FI0.0,/,
2 5X,'LIQUID DENSITY, ib/ft^3.: ' , T60, F9.3,/,
3 5X,'VAPOR DENSITY, ib/ft^3.: ' , T60, F9.3,/,
4
5X,'LIQUID VOLUMETRIC RATE, ftA3/sec.: ' , T60, F9.4,/,
5
5X,'VAPOR VOLUMETRIC RATE, ft^3/sec.: ' , T60, F9.4,/,
6
5X,'LIQUID SURGE TIME, min.:', T60, F9.3,/,
7
5X,'LENGTH TO DIAMETER RATIO (L/D):', T60, F6.1)
WRITE (i, 170) SF2, KH, QV2, VMAX2
FORMAT (5X,'SEPARATION FACTOR:',T60,F8.3,/,
5X,'VAPOR VELOCITY FACTOR:',T60,FS.3,/,
5X,'VAPOR VOLUMETRIC RATE, ftA3/s.: ' , T60, F9.3,/,
5X,'MAXIMUM VAPOR VELOCITY, ft/s.:',T60, F8.3)
WRITE (i, 180) D2, L, VESVOL, CALT2
FORMAT (5X,'VESSEL DIAMETER, ft.:',T60, F8.3,/,
5X,'VESSEL LENGTH, ft.:', T60, F8.3,/,
5X,'VESSEL VOLUME, ft^3.: ' , T60, F9.3,/,
5X,'CALCULATED LIQUID SURGE TIME, min.:', T60, F8.3)
WRITE (i, 190)
FORMAT (78(IH-))
FORM FEED THE PRINTING PAPER TO THE TOP OF THE NEXT PAGE.
WRITE (i, *) CHAR(12)
RETURN
END
305
ii
PROGRAM PROG42
********************************************************************
THIS PROGRAM CALCULATES THE SEGMENTAL AREA OF A CIRLCE COUPLED
WITH A MODIFIED DOOLITTLE FORMULA FOR DISHED HEADS TO CALCULATE
PARTIAL VOLUMES OF HORIZONTAL VESSELS.
THE PROGRAM WILL CALCULATE PARTIAL VOLUMES FOR HORIZONTAL
CYLINDRICAL VESSELS WITH FLAT, DISHED, ELLIPTICAL AND HEMISPHERICAL
HEADS, AND VERTICAL CYLINDRICAL TANKS.
********************************************************************
CL = CHORD LENGTH OF SEGMENTAL AREA, in.
AC = AREA OF CHORD, in^2.
VHC = VOLUME OF HORIZONTAL CYLINDER, in^3.
VDH = VOLUME OF DISHED HEADS, in^3.
VELL = VOLUME OF ELLIPTICAL HEADS, in^3.
VHS = VOLUME OF HEMISPHERICAL HEADS, in^3.
VT = TOTAL VOLUME OF HORIZONTAL VESSEL, in^3.
D = VESSEL, TANK, OR CIRCLE DIAMETER, in.
H = CHORD OR LIQUID HEIGHT, in.
R = RADIUS OF VESSEL OR TANK, in.
L = VESSEL LENGTH, in.
VH = HEAD VOLUMES, in^3.
BBL = VOLUME IN BARRELS
AREA = CIRCLE AREA, in^2.
REAL LI, L2, L3, L4, L5
COMMON PI
COMMON/DATA1/ DI, HI, L1
COMMON/DATA2/ D2, H2, L2
COMMON~DATA3~
D3, H3, L3
COMMON~DATA4~
D4, H4, L4
COMMON/DATA5/ D5, H5, L5
COMMON/PROGI/ VHC, VHCCFT, VHCGAL, VHCBBL
COMMON/PROG2/ VT, VTCFT, VTGAL, VTBBL
COMMON/PROG3/ VTELL, VTECFT, VTEGAL, VTEBBL
COMMON/PROG4/ VTHS, VTHCFT, VTHGAL, VTHBBL
COMMON/PROG5/ VVT, VVCFT, VVGAL, VVBBL
OPEN (UNIT=3, FILE='DATA42.DAT', STATUS='OLD'
OPEN (UNIT=l, FILE='PRN')
PI = 3.1415927
READ (3, *, ERR=I9) I
GO TO (ii, 22, 33, 44, 55), I
READ TANK DIAMETER, DI: in.
READ LIQUID DEPTH, HI: in.
READ TANK LENGTH, LI: in.
READ (3, *, ERR=I9) DI, HI, L1
, ERR=I8 )
GO TO 66
306