Coker A.K. Fortran Programs for Chemical Process Design, Analysis, and Simulation
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PROGRAM PROG36
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THIS PROGRAM WILL qALCULATE THE FROUDE NUMBERS OF VAPOR-LIQUID
TWO-PHASE VERTICAL PIPE. IT FURTHER PRINTS OUT A MESSAGE IF
THE PIPE IS SELF-VENTING, IF PULSATION FLOW OCCURS, OR IF NO
PRESSURE GRADIENT IS NEEDED.
***************************************************************
AREA
D
FRNL
FRNG
G
DENL
VL
VG
WL
WG
= INSIDE CROSS-SECTIONAL AREA OF PIPE, ft^2.
= INSIDE DIAMETER OF PIPE, inch.
= FROUDE NUMBER FOR LIQUID PHASE
= FROUDE NUMBER FOR GAS PHASE
= GRAVITATIONAL CONSTANT (32.2 ft/s^2)
= LIQUID DENSITY, ib/ft^3
= LIQUID VELOCITY, ft/s.
= VAPOR VELOCITY, ft/s.
= LIQUID FLOWRATE, ib/h.
= VAPOR FLOWRATE, ib/h.
OPEN FILES TO READ THE DATA AND TO PRINT THE RESULTS
PARAMETER (G = 32.2, PI = 3.1415927)
OPEN THE DATA FILE.
OPEN (UNIT = 3, FILE = 'DATA36.DAT', STATUS = 'OLD', ERR = 18)
OPEN FILE FOR PRINTING THE RESULTS.
OPEN (UNIT = i, FILE = 'PRN')
WRITE (i, i00)
FORMAT (///,15X, 'VAPOR-LIQUID TWO-PHASE VERTICAL DOWNFLOW',/IH ,
78(IH*))
READ THE INPUT DATA
READ THE PIPE INSIDE DIAMETER, inch: D
READ THE LIQUID FLOW RATE, Ib/hr.: WL
READ THE LIQUID DENSITY, ib/ft^3: DENL
READ THE GAS FLOW RATE, ib/hr.: WG.
READ THE GAS DENSITY, Ib/ft^3.: DENG.
READ (3, *
READ (3, *
GO TO i0
, ERR=I9) D, WL, DENL
, ERR=I9) WG, DENG
WRITE (*, II0)
FORMAT (5X, 'DATA FILE DOES NOT EXIST')
GO TO 999
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WRITE (*, 120)
FORMAT (5X,'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
D1 = D/12.
AREA = (PI*DI**2)/4.0
WRITE (i, 130) D
FORMAT (10X, 'PIPE INTERNAL DIAMETER, inch:', T65, F8.3)
WRITE (i, 140) WL, DENL
FORMAT (10X, 'LIQUID FLOWRATE, ib/h.:', T65, F8.0, /, 10X,
'LIQUID DENSITY, ib/ft^3: ' , T65, F8.3)
WRITE (i, 150) WG, DENG
FORMAT (10X, 'VAPOR FLOWRATE, Ib/h.:', T65, F8.0, /, 10X,
'VAPOR DENSITY, ib/ft^3: ' , T65, F8.3)
WRITE (I, 160) AREA
FORMAT (10X, 'PIPE AREA, ft^2: ' , T65, F8.3)
CALCULATE LIQUID AND VAPOR VELOCITIES
VL = WL/(3600.0*DENL*AREA)
VG = WG/(3600.0*DENG*AREA)
WRITE (i, 170) VL, VG
FORMAT (10X, 'LIQUID VELOCITY, ft/s:', T65, F8.3, /, 10X,
'VAPOR VELOCITY, ft/s:', T65, F8.3)
CALCULATE THE LIQUID PHASE AND THE VAPOR PHASE FROUDE NUMBERS
FRNL = (VL/((G*DI)**0.5))*(DENL/(DENL-DENG))**0.5
FRNG = (VG/((G*DI)**0.5))*(DENG/(DENL-DENG))**0.5
WRITE (i, 180) FRNL, FRNG
FORMAT (10X, 'FROUDE NUMBER FOR LIQUID PHASE:', T65, F8.4, /,
10X, 'FROUDE NUMBER FOR VAPOR PHASE:', T65, F8.4)
TEST FOR SELF-VENTING, PULSE FLOW OR NO PRESSURE GRADIENT.
IF ( FRNL .LT. 0.31) THEN
WRITE (i, 190)
FORMAT (10X, 'LINE IS SELF-VENTING THEREFORE NO VIBRATION',k )
WRITE (i, 200)
FORMAT (' PROBLEMS ARE EXPECTED')
ELSEIF ( FRNL .GE. 0.31 .AND. FRNL .LT. 1.0) THEN
WRITE (i, 210)
FORMAT (10X, 'FLOW IS PULSE AND THIS MAY RESULT IN PIPE'\,)
WRITE (i, 220)
FORMAT (' VIBRATION')
ELSEIF ( FRNL .GT. 1.0) THEN
WRITE (i, 230)
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999
FORMAT (IOX, 'NO PRESSURE GRADIENT')
ENDIF
WRITE (i, 240)
FORMAT (78(IH-))
FORM FEED THE PRINTING PAPER TO TOP OF THE NEXT PAGE.
WRITE (I, *) CHAR(12)
CLOSE (3, STATUS = 'KEEP')
CLOSE (i)
STOP
END
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PROGRAM PROG37
i00
******************************************************************
THIS PROGRAM CALCULATES LINE SIZES FOR FLASHING STEAM CONDENSATE.
THE PROGRAM WILL COMPUTE THE FOLLOWING:
i. CALCULATES THE AMOUNT OF CONDENSATE FLASHED FOR ANY GIVEN
CONDENSATE HEADER PRESSURE FROM 15 TO 140 psia. AND INITIAL
STEAM PRESSURES MAY VARY BETWEEN 40 AND 165 psia.
2. THE RETURN CONDENSATE HEADER TEMPERATURE.
3. THE PRESSURE DROP (psi/100ft.) OF THE STEAM CONDENSATE
MIXTURE IN THE RETURN HEADER.
4. THE VELOCITY OF THE STEAM CONDENSATE MIXTURE AND
5. INDICATES A WARNING MESSAGE IF VELOCITY IS EQUAL TO OR
GREATER THAN 5000 ft/min.
NOMENCLATURE.
n =
DELTP =
DENG =
DENL =
DENMIX =
FF =
PC =
PH =
TFL =
VEL =
W =
WFRFL =
WG =
WL =
PIPE INTERNAL DIAMETER, inch.
PRESSURE DROP OF FLASHED CONDENSATE MIXTURE,
psi/10Oft.
FLASHED STEAM DENSITY, Ib/ft^3.
FLASHED CONDENSATE LIQUID DENSITY, ib/ft^3.
DENSITY OF MIXTURE (FLASHED CONDENSATE/STEAM)
ib/ft^3.
FRICTION FACTOR.
STEAM CONDENSATE PRESSURE BEFORE FLASHING, psia.
FLASHED CONDENSATE HEADER PRESSURE, psia.
TEMPERATURE OF FLASHED CONDENSATE, oF.
VELOCITY OF FLASHED CONDENSATE MIXTURE, ft/min.
TOTAL FLOW OF MIXTURE IN CONDENSATE HEADER, Ib/h.
WEIGHT FRACTION OF CONDENSATE FLASHED TO VAPOR.
FLASHED STEAM FLOWRATE, ib/h.
FLASHED CONDENSATE LIQUID FLOWRATE, ib/h.
***************************************************************
OPEN FILES TO READ THE DATA AND TO PRINT THE RESULTS
OPEN ( UNIT = 3, FILE = 'DATA37.DAT', STATUS = 'OLD', ERR = 18)
OPEN (UNIT = i, FILE = 'PRN')
WRITE (i, i00)
FORMAT (///, 15X, 'LINE SIZING FOR FLASHING STEAM CONDENSATE',/,
VS(ZH*))
READ THE INPUT DATA
READ THE PIPE INTERNAL DIAMETER, inch: D
READ THE FLUID FLOW RATE, ib/hD.: W
READ THE CONDENSATE STEAM PRESSURE BEFORE FLASHING, psia.: PC
READ THE FLASHED CONDENSATE HEADER PRESSURE, psia.: PH
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READ (3, *, ERR=I9) D, W
READ (3, *, ERR=I9) PC, PH
GO TO i0
WRITE (*, ii0)
FORMAT (10X, 'DATA FILE DOES NOT EXIST')
GO TO 999
WRITE (*, 1207
FORMAT (10X, 'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
X = 6.122 - (16.919/ALOG(PH))
A = 0.00671*(ALOG(PH) 7**2.27
B = EXP(X)*(10**(-4)) + 0.0088
CALCULATE WEIGHT FRACTION OF CONDENSATE FLASHED TO VAPOR.
WFRFL = B*(ALOG(PC))**2 - A
CALCULATE FLASHED STEAM FLOWRATE AND FLASHED STEAM
CONDENSATE LIQUID FLOWRATE, ib/h.
WG = WFRFL*W
WL = W - WG
WRITE (i, 130) D, W
FORMAT (10X, 'PIPE INTERNAL DIAMETER, inch:', T65, F8.3, /,
*
10X,'TOTAL FLOW OF MIXTURE IN CONDENSATE HEADER, ib/h:',
* T65, F8.0)
WRITE (i, 140) PC, PH
FORMAT (10X,'STEAM CONDENSATE PRESSURE BEFORE FLASHING, psia:',
* T65, F8.3, /, 10X,'FLASHED CONDENSATE HEADER PRESSURE, psia:',
* T65, F8.3)
WRITE (i, 150) WFRFL
FORMAT (10X,'WEIGHT FRACTION OF CONDENSATE FLASHED TO VAPOR:',
* T65, F8.3)
WRITE (I, 160) WG, WL
FORMAT (10X, 'FLASHED STEAM FLOWRATE, ib/h.:', T65, F8.0,/,
* 10X,'FLASHED CONDENSATE LIQUID FLOWRATE, ib/h.:', T65, FS.0)
CALCULATE
THE TEMPERATURE OF FLASHED CONDENSATE.
TFL = I15.68"(PH)**0.226
CALCULATE THE FLASHED STEAM DENSITY, FLASHED CONDENSATE LIQUID
DENSITY AND DENSITY OF MIXTURE (FLASHED CONDENSATE/STEAM) ib/ft^3
DENG = 0.0029"(PH)**0.938
DENL = 60.827-(0.078*PH)+(0.00048*(PH)**2)-(0.0000013*(PH)**3)
DENMIX = W/(WG/DENG + WL/DENL)
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FOR TURBULENT FLOW, CALCULATE THE FRICTION FACTOR.
FF = 0.25/(-ALOGI0(0.000486/D))**2
DELTP = (0.000336*FF*W**2)/(DENMIX*D**5)
CALCULATE THE VELOCITY OF FLASHED CONDENSATE MIXTURE, ft/min.
VEL = (3.054/D**2)*(WG/DENG + WL/DENL)
WRITE (i, 170) TFL, DENG
FORMAT (10X, 'TEMPERATURE OF FLASHED CONDENSATE, oF:', T65,
F8.3, /, 10X, 'FLASHED STEAM DENSITY, ib/ft^3: 9 , T65, F8.3)
WRITE (i, 180) DENL, DENMIX
FORMAT (10X, "FLASHED CONDENSATE LIQUID DENSITY, ib/ft^3: " ,
T65, F8.3, /, 10X, 'DENSITY OF MIXTURE, Ib/ft^3: ' , T65, F8.3)
WRITE (I, 190) FF, DELTP, VEL
FORMAT (10X, 'FRICTION FACTOR:', T65, F8.4, /, 10X,
*
'PRESSURE DROP OF FLASHED, psi:',/,10X,
*
'CONDENSATE MIXTURE, psi/100ft:', T65,
* F8.3,/,10X, 'VELOCITY OF FLASHED CONDENSATE MIXTURE, ft/min.:'
* T65, FI0.0)
DETERMINE WHETHER PROCESS LINE MAY DETERIORATE i.e. WHETHER
VELOCITY IS EQUAL OR GREATER THAN 5000 ft./min.
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999
IF ( VEL .GE. 5000.0) THEN
WRITE (i, 200)
FORMAT (10X, 'FLASHED CONDENSATE MIXTURE VELOCITY IS GREATER',\)
WRITE (i, 210)
FORMAT (' THAN 5000 ft./min.')
WRITE (i, 220)
FORMAT (10X, "DETERIORATION OF THE LINE IS POSSIBLE')
ELSE
WRITE (I, 230)
FORMAT (10X, 'FLASHED CONDENSATE MIXTURE IS LESS THAN',\)
WRITE (I, 240)
FORMAT (' 5000 ft/min.')
WRITE (i, 250)
FORMAT (IOX,'THE CONDENSATE HEADER LINE WILL NOT DETERIORATE')
ENDIF
WRITE (i, 260)
FORMAT (78(IH-))
FORM FEED THE PRINTING PAPER TO TOP OF THE NEXT PAGE.
WRITE (i, *) CHAR(12)
CLOSE (3, STATUS = 'KEEP')
CLOSE (i)
STOP
END
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PROGRAM PROG38
I00
THIS PROGRAM CALCULATES THE TOTAL PRESSURE DROP IN A PACKED BED
WHEN LIQUID OR VAPOR STREAMS ARE PASSED THROUGH IT. THE
PROGRAM ALSO CALCULATES THE FLUID REYNOLDS NUMBER AND THE
FRICTION FACTOR.
****************************************************************
NOMENCLATURE
A
AP
BD
BL
DEN
DELPT
FV
FP
G
GC
MW
P
PD
PL
RE
S
T
VIS
W
= CROSS-SECTIONAL AREA OF BED, ft^2.
= AREA OF PARTICLES, ft^2.
= PACKED BED DIAMTER, ft.
= PACKED BED LENGTH, ft.
= DENSITY OF FLUID AT FLOWING CONDITIONS, Ib/ft^3.
= TOTAL PRESSURE DROP IN PACKED BED, ib/in^2.
= FRACTION VOIDS IN PACKED BED.
= FRICTION FACTOR.
= SUPERFICIAL MASS VELOCITY Ib/h.ft^2.
= GRAVITATIONAL CONSTANT = 4.17 x 10^8 (ibm/ibf)(ft/h^2)
= MOLECULAR WEIGHT OF FLUID.
= FLUID PRESSURE, psia.
= PARTICLE DIAMETER, inch.
= PARTICLE LENGTH, inch.
= REYNOLDS NUMBER
= PACKED BED SURFACE AREA, (ft^2/ft^3 BED).
= FLUID TEMPERATURE, oR.
= FLUID VISCOSITY, cP.
= FLUID FLOWRATE, Ib/h.
Z =
COMPRESSIBILITY FACTOR
( Z=I.O)
**************************************************************
PARAMETER ( PI = 3.1415927, GC = 4.17,10,,8)
OPEN FILES TO READ THE DATA AND TO PRINT THE RESULTS.
OPEN (UNIT = 3, FILE ='DATA38.DAT', STATUS = 'OLD', ERR = 18)
OPEN (UNIT = i, FILE = 'PRN')
WRITE (i, i00)
FORMAT (///, 25X,'PRESSURE DROP IN A PACKED BED',/IH ,
78(IH*))
READ THE DATA VALUES.
READ THE PACKED BED DIAMERTER, ft. : BD
READ THE PACKED BED LENGTH, ft. : BL
READ THE FLUID FLOW RATE, ib/hr.. : W
READ THE PARTICLE DIAMETER, inch: PD
READ THE PARTICLE LENGTH, inch: PL
READ THE FRACTION OF VOIDS IN PACKED BED, inch: FV
READ THE DENSITY OF FLUID AT FLOWING CONDITION, Ib/ft^3. : DEN
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READ THE FLUID VISCOSITY, cP: VIS
READ (3, *, ERR=I9) BD, BL, W
READ (3, *, ERR=I9) PD, PL, FV
READ (3, *, ERR=I9) DEN, VIS
GO TO i0
WRITE (*, ii0)
FORMAT (10X, 'DATA FILE DOES NOT EXIST')
GO TO 999
WRITE (*, 120)
FORMAT (10X, 'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
WRITE (i, 130) BD, BL, W
FORMAT (10X, 'PACKED BED DIAMETER, ft.:', T60, F8.3, /, 10X,
'LENGTH OF PACKED BED, ft.:', T60, F8.3, /, 10X,
'FLUID FLOWRATE THROUGH PACKED BED, ib/h.:', T60, FI0.1)
WRITE (i, 140) PD, PL, FV
FORMAT (10X, 'PARTICLE DIAMETER, inch.:' T60, F8.3, /, 10X,
'PARTICLE LENGTH, inch.:', T60, F8.3, /, 10X,
'FRACTIONAL VOIDS IN PACKED BED:', T60, F8.3)
WRITE (i, 150) DEN, VIS
FORMAT (10X, 'DENSITY OF FLUID, Ib/ft^3: ' , T60, F8.4, /, 10X,
'FLUID VISCOSITY, cP:', T60, F8.4)
CALCULATE THE CROSS-SECTIONAL AREA OF BED, ft^2.
A = (PI*BD**2)/4.0
CALCULATE THE SUPERFICIAL MASS VELOCITY, W/A
S = W/A
CALCULATE THE AREA OF PARTICLES AND THE VOLUME OF PARTICLES.
AP = (I.0/144.0)*((PI*PD**2)/2.0 + (PI*PD*PL))
VP = (I.0/1728.0)*(((PD**2)*PI*PL)/4.0)
CALCULATE THE PACKED BED SURFACE AREA, ft^2/ft^3. BED.
S = AP*(I - FV)/VP
CALCULATE
THE EFFECTIVE PARTICLE DIAMETER, ft.
DP = 6.0*(I-FV)/S
CALCULATE THE FLUID REYNOLDS NUMBER, RE
RE = (G*DP)/(2.419*VIS*(I.0 - FV))
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C
999
WRITE (i, 160) A, G
FORMAT (10X, 'CROSS-SECTIONAL AREA OF BED, ft^2: ' , T60, F8.4,
/, 10X, 'SUPERFICIAL MASS VELOCITY, ib/h.ft^2: ' , T60,
F8.1)
WRITE (i, 170) AP, VP
FORMAT (10X, 'AREA OF PARTICLES, ft^2: ' , T60, E12.4, /, 10X,
'VOLUME OF PARTICLES, ft^3: " , T60, E12.4)
WRITE (i, 180) S, DP
FORMAT (10X, 'THE PACKED BED SURFACE AREA, ft^2/ft^3 BED:',
T60, F8.3, /, 10X,'EFFECTIVE PARTICLE DIAMETER, ft.:',T60, F8.4)
WRITE (i, 190) RE
FORMAT (10X, 'FLUID REYNOLDS NUMBER:', T60, FI0.0)
DETERMINE THE FRICTION FACTOR FOR LAMINAR, INTERMEDIATE OR
TURBULENT FLOW.
IF (RE .LT. 1.0) THEN
FP = 150.0/RE
WRITE (I, 200) FP
FORMAT (IOX, 'FRICTION FACTOR FOR LAMINAR FLOW:'
ELSEIF (RE .GT. 1.0 .AND. RE .LT. 10"'4) THEN
, T60, F8.4)
FP = 150.0/RE+1.75
WRITE (i, 210) FP
FORMAT (10X, 'FRICTION FACTOR FOR INTERMEDIATE FLOW: ', T60,
F8.4)
ELSEIF (RE .GT. 10"'4) THEN
FP = 1.75
WRITE (I, 220)
FORMAT (10X,'FRICTION FACTOR FOR TURBULENT FLOW:', T60, F8.2)
ENDIF
CALCULATE THE TOTAL PRESSURE DROP IN PACKED BED, DELTP.
VALI = (BL*(I-FV)*G**2)/(144.0*(FV**3)*DP*GC*DEN)
VAL2 = ((150.0*2.419*VIS*(I.0-FV)/(DP*G))+I.75)
DELTP = VALI * VAL2
WRITE (I, 230) DELTP
FORMAT (10X, 'TOTAL PRESSURE DROP IN PACKED BED, ib/in^2: '
T60, F8.3)
WRITE (i, 240)
FORMAT (78(IH-))
FORM FEED THE PRINTING PAPER TO TOP OF THE NEXT PAGE.
WRITE (i, *) CHAR(12)
CLOSE (3, STATUS = 'KEEP')
CLOSE (i)
STOP
END
255
CHAPTER 4
Equipment Sizing
INTRODUCTION
The process engineer is often required to design separators or knock-
out drums for removing liquids from process gas streams. This chapter
reviews the design of horizontal and vertical separators and the sizing
of partly filled horizontal and cylindrical vessels. The chapter concludes
by reviewing the sizing of a cyclone and a solid-desiccant gas dryer.
Vessels used for processing in the chemical process industries (CPI)
are principally of two kinds: those that are without internals and those
with internals. Empty separators are drums that provide intermediate
storage or surge of a process stream for a limited or extended period.
Alternatively, they provide phase separation by settling.
The second category comprises equipment such as reactors, mixers,
distillation columns, and heat exchangers. In some cases, it is important
to separate liquid and gas flowing simultaneously through a pipe. This
is because the conditions of the flowing mixture and the efficiency of
separation may vary widely. Therefore, a separator for such duty must
be adequate. In addition, there are constraints due to space or weight
that often affect the choice of separators, the need to handle solids or
effect a three-phase separation, and the requirements for liquid hold-up.
In practice, most separation problems are solved by the following types
of separating equipment.
Knockout or Surge Drums (Figures 4-1 and 4-2). A
knockout drum
is suitable for a bulk separation of gas and liquid, particularly when the
liquid volume fraction is high with stratified or plug flow in the pipe.
Also, it is useful when vessel internals are required to be kept to a
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