Coker A.K. Fortran Programs for Chemical Process Design, Analysis, and Simulation
Подождите немного. Документ загружается.
PROGRAM PROG83
C
C
C
C
C
C
C
C
C
C
C
C
C HI =
C K =
C RE =
C PR =
C DEQ =
C VIS =
C VISW =
C VIST =
C VISS =
C VISF =
C J =
C G =
C CP =
C AREA =
C IDT =
C IDF =
C FOL =
C HIF =
C
C IDS =
C ODT =
C DELTW =
C KT =
C AI =
C AO =
C
C UO =
C NFA =
C AF =
C X =
C FE =
C ESEF =
C HIFD =
C TDEN =
C SDEN =
C NTP =
C NSP =
C NFP =
C FOLT =
C FOLS =
C FOLF =
C FTTUBE =
C FTSHELL =
C FLUIDT =
THIS PROGRAM RATES DOUBLE PIPE HEAT EXCHANGERS USING
BARE TUBES OR LONGITUDINAL FINNED TUBES.
THE PROGRAM CALCULATES THE HEAT LOAD, THE LOG MEAN TEMPERATURE
DIFFERENCE FOR COUNTER CURRENT FLOW, THE CORRECTED FILM HEAT TRANSFER
COEFFICIENTS IN BOTH THE TUBE AND THE SHELL SIDES, THE OVERALL HEAT
TRANSFER COEFFICIENT AND THE HEAT TRANSFER SURFACE. THE PROGRAM
FURTHER CALCULATES THE FRICTION FACTOR (Using correlations given by
Dennis Wright: Basic Programs for chemical engineers, Van Nostrand
Reinhold Company, NY 1986) AND THE PRESSURE DROP IN THE TUBE AND THE
SHELL SIDES OF THE DOUBLE PIPE HEAT EXCHANGERS.
********************************************************************
HEAT-TRANSFER FILM COEFFICIENT, Btu/ft^2 oF.h
FLUID THERMAL
CONDUCTIVITY,
Btu/ft.h.oF
REYNOLDS NUMBER
PRANDTL NUMBER
EQUIVALENT DIAMETER, ft.
FLUID VISCOSITY (FLOWING), cP.
FLUID VISCOSITY (AT WALL), cP.
FLUID VISCOSITY (TUBE SIDE), cP.
FLUID VISCOSITY (SHELL SIDE - bare tube), cP.
FLUID VISCOSITY (SHELL SIDE - finned tube), cP.
HEAT-TRANSFER FACTOR
MASS FLOW RATE, Ib/h.ft^2.
FLUID SPECIFIC HEAT, Btu/ib.oF.
HEAT TRANSFER SURFACE AREA, ft^2.
INSIDE-TUBE DIAMETER, in.
INSIDE DIAMETER (finned tube), in.
FOULING FACTOR
HEAT-TRANSFER FILM COEFFICIENT CORRECTED
FOR FOULING, Btu/ft^2.oF.h.
INSIDE SHELL DIAMETER, in.
OUTSIDE TUBE DIAMETER, in.
TUBE WALL THICKNESS, ft.
THERMAL CONDUCTIVITY OF TUBE MATERIAL, Btu/ft.h.oF.
INSIDE HEAT-TRANSFER AREA-TUBE, ft^2/ft.
OUTSIDE HEAT-TRANSFER AREA-TUBE, ft^2/ft (FOR FINNED
TUBES INCLUDES FIN AREA).
OVERALL HEAT-TRANSFER COEFFICIENT, Btu/h.ft^2.oF.
NET FREE CROSS-SECTIONAL AREA, SHELL SIDE, ft^2.
FINNED TRANSFER AREA, ft^2 .
PARAMETER USED IN FIN EFFICIENCY CALCULATION
FIN EFFICIENCY (%).
EFFECTIVE SURFACE EFFICIENCY FOR FINS (%).
CORRECTED FILM HEAT-TRANSFER RATE, Btu/ft^2.h.oF
TUBE SIDE FLUID DENSITY, Ib/ft^3.
SHELL SIDE FLUID DENSITY, ib/ft^3.
NUMBER OF TUBE PASSES.
NUMBER OF SHELL PASSES (bare-tube).
NUMBER OF SHELL PASSES (finned-tube).
FOULING FACTOR OF THE TUBE SIDE.
FOULING FACTOR OF THE SHELL SIDE (bare-tube).
FOULING FACTOR OF THE SHELL SIDE (finned-tube).
FLUID NAME IN THE TUBE SIDE.
FLUID NAME IN THE SHELL SIDE
FLUID PHASE FLOW IN THE TUBE SIDE.
697
9
C
Ii
FLUIDS = FLUID PHASE FLOW IN THE SHELL SIDE.
TUBE = CHECKS TO DETERMINE WHETHER THE DOUBLE PIPE HEAT
EXCHANGER IS BARE-TUBED OR FINNED-TUBE.
LMTD = LOG MEAN TEMPERATURE DIFFERENCE (oF).
TL = TUBE LENGTH, ft.
WT = FLUID FLOWRATE TUBE SIDE, Ib/hr.
WS = FLUID FLOWRATE SHELL SIDE (BARE-TUBE), Ib/hr.
WF = FLUID FLOWRATE SHELL SIDE (FINNED-TUBE), Ib/hr.
CHARACTER*30 FLUIDT, FLUIDS, FLUIDF, TUBE, FTTUBE, FTSHELL
EXTERNAL HTFCV,HTFCL,HTFCJ
REAL IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
REAL IDT,ODT,KT
REAL IDS,ODS,KS,KST
REAL IDF,ODF,KF,KFT
REAL LMTD
COMMON TUBE
COMMON/DATA/FTTUBE, FTSHELL, TDEN, SDEN
COMMON/DATAI/FLUIDT,IDT,ODT,WT,CPT,VIST,KT,TTI,TT2,FOLT,TL,NTP
COMMON/DATA2/FLUIDS,IDS,ODS,WS,CPS,VISS,KS,TSI,TS2,FOLS,KST,NSP
COMMON/DATA3/FLUIDF,IDF,ODF,WF,CPF,VISF,KF,TFI,TF2,FOLF,
* FHT,FTHICK,NF,KFT,NFP
COMMON/DATA4/ PI
COMMON/DATA5/ IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
COMMON/RESI/VELT,RET,PRT,FRICTT,DROPT,HTFT,HIFTU
COMMON/RES2/VELS,RES,PRS,FRICTS,DROPS,HTFS,HIFS
COMMON/RES3/VELF,REF,PRF,FRICTF,DROPF,HTFF,HIFF,X,FE,ESEF,HIFD,
* UO
COMMON/RES4/ LMTD, AREA, Q
OPEN (UNIT=3, FILE='DATA83.DAT', STATUS='OLD', ERR=I8)
OPEN (UNIT= i, FILE='PRN')
PI = 3.1415927
TUBE-SIDE HEAT-TRANSFER CALCULATIONS
INPUT NAME OF FLUID IN THE TUBE SIDE
READ (3, 9, ERR=I9) FTTUBE
FORMAT (A)
INPUT FLUID PHASE FLOW (e.g. liquid/vapor)
READ (3, ii, ERR=I9) FLUIDT
FORMAT ( A )
READ THE INSIDE TUBE DIAMETER, inch.: IDT
READ THE OUTSIDE TUBE DIAMETER, inch.: ODT
READ THE FLUID FLOWRATE IN THE TUBE SIDE, ib/hr.: WT
READ THE FLUID SPECIFIC HEAT CAPACITY, Btu/Ib.oF.: CPT
READ THE FLUID VISCOSITY, cP: VIST
READ THE FLUID THERMAL CONDUCTIVITY, KT: Btu/hr.ft.oF: KT
698
C
C
C
5
14
22
34
READ THE FLUID INLET TEMPERATURE, oF: TTI
READ THE FLUID OUTLET TEMPERATURE, oF: TT2
READ THE TUBE SIDE FOULING FACTOR: FOLT
READ THE TUBE SIDE FLUID DENSITY, Ib/ft^3: TDEN
READ THE TUBE LENGTH, ft.: TL
READ THE NUMBER OF TUBE PASSES: NTP
READ (3, *
READ (3, *
READ (3, *
READ (3, *
GO TO i0
, ERR=I9) IDT, ODT, WT
, ERR=I9) CPT, VIST, KT
, ERR=I9) TTI, TT2, FOLT
, ERR=I9) TDEN, TL, NTP
CHECK WHETHER THE HEAT EXCHANGER IS BARE-TUBE OR FINNED-TUBE
i.e., WHETHER THE HEAT EXCHANGER HAS FINS
INPUT NAME OF FLUID IN THE SHELL SIDE
READ ( 3, 14, ERR=I9) FTSHELL
FORMAT (A)
READ (3, 22, ERR=I9) TUBE
FORMAT (A)
IF (TUBE .EQ. 'FINS' .OR. TUBE .EQ. 'fins') THEN
GO TO 33
ELSEIF (TUBE .EQ. 'BARE-TUBE'.OR. TUBE .EQ. 'bare-tube') THEN
READ DATA VALUES FOR THE SHELL-SIDE BARE-TUBE
INPUT FLUID PHASE FLOW (e.g. liquid/vapor)
READ (3, 34, ERR=I9) FLUIDS
FORMAT(A)
READ THE INSIDE DIAMETER, inch.: IDS
READ THE OUTSIDE DIAMETER, inch.: ODS
READ THE FLUID FLOWRATE, ib/hr.: WS
READ THE FLUID SPECIFIC HEAT CAPACITY, Btu/Ib.oF: CPS
READ THE FLUID VISCOSITY, cP.: VISS
READ THE FLUID THERMAL CONDUCTIVITY, Btu/ft.hr.oF: KS
READ THE FLUID INLET TEMPERATURE, oF: TSI
READ THE FLUID OUTLET TEMPERATURE, oF: TS2
READ THE SHELL SIDE FOULING FACTOR: FOLS
READ THE TUBE THERMAL CONDUCTIVITY, Btu/ft.hr.oF: KST
READ THE FLUID DENSITY, ib/ft^3.: SDEN
READ THE NUMBER OF SHELL PASSES: NSP
READ (3, *
READ (3, *
READ (3, *
READ (3, *
, ERR=I9) IDS, ODS, WS
, ERR=I9) CPS, VISS, KS
, ERR=I9) TSI, TS2, FOLS
, ERR=I9) KST, SDEN, NSP
699
C
C
33
44
18
i00
19
ENDIF
CALCULATE THE LOG MEAN TEMPERATURE DIFFERENCE, LMTD (oF)
CALL LOGMTD (TSI, TS2, TTI, TT2, LMTD)
GO TO 20
READ DATA VALUES FOR THE SHELL-SIDE FINNED TUBE
INPUT PHASE FLOW OF FLUID IN THE SHELL SIDE (e.g. Liquid/vapor)
READ (3, 44, ERR=I9) FLUIDF
FORMAT ( A )
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
READ THE
NUMBER OF FINS: NF
INSIDE DIAMETER, inch.: IDF
OUTSIDE DIAMETER, inch.: ODF
FLUID FLOWRATE, ib/hr.: WF
FLUID SPECIFIC HEAT, Btu/ib.oF: CPF
FLUID VISCOSITY, cP.: VISF
FLUID THERMAL CONDUCTIVITY, Btu/hr.ft.oF: KF
FLUID INLET TEMPERATURE, oF: TFI
FLUID OUTLET TEMPERATURE, oF: TF2
FLUID FOULING FACTOR: FOLF
FINS HEIGHT, inch.: FHT
FINS THICHNESS, inch.: FTHICK
TUBE SIDE THERMAL CONDUCTIVITY, Btu/hr.ft.oF: KFT
FLUID DENSITY, ib/ft^3: SDEN
NUMBER OF PASSES: NFP
READ (3, *
READ (3, *
READ (3, *
READ (3, *
READ (3, *
READ (3, *
, ERR=I9) NF
, ERR=f9) IDF, ODF, WF
, ERR=f9) CPF, VISF, KF
, ERR=f9) TFI, TF2, FOLF
, ERR=f9) FHT, FTHICK
, ERR=f9) KFT, SDEN, NFP
CALCULATE THE LOG MEAN TEMPERATURE DIFFERENCE, LMTD (oF)
CALL LOGMTD (TFI, TF2, TTI, TT2, LMTD)
CALCULATE THE HEAT LOAD ON UNIT, Btu/hr.
Q = WF*CPF*(TFI-TF2)
SHELL-SIDE CALCULATIONS (FINNED-TUBE)
GO TO 30
WRITE (*, I00)
FORMAT(//,6X,'DATA FILE DOES NOT EXIST')
GO TO 999
WRITE (*, ii0)
700
ii0
C
i0
C
20
C
30
C
40
999
FORMAT(//,6X,'ERROR MESSAGE IN THE DATA VALUE')
GO TO 999
TUBE-SIDE CALCULATIONS
CALL PROGI
GO TO 5
SHELL-SIDE
CALCULATIONS
(BARE-TUBE)
CALL PROG2
GO TO 40
SHELL-SIDE CALCULATIONS (FINNED-TUBE)
CALL PROG3
CALCULATE THE HEAT TRANSFER SURFACE AREA, (AREA, ft^2).
AREA = Q/(UO*LMTD)
CALL RESULTS
CLOSE ( 3, STATUS='KEEP' )
CLOSE (i)
STOP
END
*****************************************************************
PROGRAM CALCULATES HEAT-TRANSFER FILM COEFFICIENT IN THE TUBE
SIDE HEAT EXCHANGER
*****************************************************************
SUBROUTINE PROGI
CHARACTER*30 FLUIDT, FTTUBE, FTSHELL,FLUIDF
REAL IDT, ODT, KT
REAL IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
REAL IDF, ODF, KF, KFT
COMMON/DATA/FTTUBE, FTSHELL, TDEN, SDEN
COMMON/DATAI/FLUIDT,IDT,ODT,WT,CPT,VIST,KT,TTI,TT2,FOLT,TL,NTP
COMMON/DATA3/FLUIDF,IDF,ODF,WF,CPF,VISF,KF,TFI,TF2,FOLF,
* FHT,FTHICK,NF,KFT,NFP
COMMON/DATA4/PI
COMMON/DATAL/IDTF,
IDSF, IDFF, ODTF, ODSF, ODFF
COMMON/RESI/VELT,RET,PRT,FRICTT,DROPT,HTFT,HIFTU
IDTF = IDT/12.0
ODTF = ODT/12.0
DEQT = IDTF
CALCULATE THE CROSS-SECTIONAL AREA OF TUBE
701
30
50
AT = (PI*IDTF**2)/4.0
CALCULATE THE MASS VELOCITY, ib/ft^2.hr.
ST = WT/AT
CALCULATE THE FLUID VELOCITY, ft./sec.
VELT = GT/(3600.0*TDEN)
CALCULATE THE REYNOLDS NUMBER
RET = (GT*DEQT)/(2.42*VIST)
CALCULATE THE PRANDTL NUMBER
PRT = (CPT*2.42*VIST)/KT
CALCULATE THE FRICTION FACTOR (Dennis Wright: Basic Programs
for chemical engineers: Van Nostrand Reinhold Company, NY 1986).
IF (RET .GT. 2100.0) THEN
FRICTT = 0.00033/(RET**0.2)
ELSEIF (RET .LT. 2100.0 ) THEN
FRICTT = 16/RET
ENDIF
CALCULATE
THE PRESSURE DROP
DROPT = (4.0*FRICTT*TL*NTP*(GT/3600.0)**2)/(64.4*TDEN*DEQT)
CHECK WHETHER FLUID IN THE TUBE SIDE IS LIQUID OR VAPOR.
IF (FLUIDT .EQ. "LIQUID'.OR. FLUIDT .EQ. 'liquid') THEN
GO TO 30
ELSEIF (FLUIDT .EQ. 'VAPOR' .OR. FLUIDT .EQ. "vapor') THEN
CALCULATE THE HEAT-TRANSFER FILM COEFFICIENT IN THE VAPOR STATE
HTFT = HTFCV (CPT,GT,DEQT)
ENDIF
GO TO 90
IF(RET .LT. 2100.0) THEN
GO TO 50
ELSE
HTFT = HTFCL (RET,PRT,KT,DEQT)
ENDIF
GO TO 90
HTFT = HTFCJ (RET, PRT, KT, DEQT, TL)
702
90
CALCULATE THE HEAT-TRANSFER FILM COEFFICIENT CORRECTED FOR
FOULING, Btu/hr.ft^2.oF
HIFTU = HTFT/(I.0+HTFT*FOLT)
RETURN
END
PROGRAM CALCULATES HEAT-TRANSFER FILM COEFFICIENT IN THE SHELL
SIDE (BARE-TUBE) AND THE OVERALL HEAT TRANSFER COEFFICIENT OF
THE HEAT EXCHANGER
SUBROUTINE PROG2
CHARACTER*30 FLUIDS, FLUIDT, FTSHELL,FTTUBE
REAL IDS, IDT, ODS, ODT, KS, KT
REAL IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
REAL LMTD
COMMON/DATA/FTTUBE,
FTSHELL, TDEN, SDEN
COMMON/DATAI/FLUIDT,IDT,ODT,WT,CPT,VIST,KT,TTI,TT2,FOLT,TL,NTP
COMMON/DATA2/FLUIDS,IDS,ODS,WS,CPS,VISS,KS,TSI,TS2,FOLS,KST,NSP
COMMON/DATA4/PI
COMMON/DATA5/IDTF,
IDSF, IDFF, ODTF, ODSF, ODFF
COMMON/RESl/VELT,RET,PRT,FRICTT,DROPT,HTFT,HIFTU
COMMON/RES2/VELS,RES,PRS,FRICTS,DROPS,HTFS,HIFS
COMMON/RES4/LMTD, AREA, Q
IDSF = IDS/12.0
ODSF = ODS/12.0
DEQS = IDSF-ODTF
RATIO1 = IDT/ODT
CALCULATE THE CROSS-SECTIONAL AREA
AS = (PI*IDSF**2)/4.0
CALCULATE THE MASS VELOCITY, Ib/ft^2.hr.
GS = WS/AS
CALCULATE THE FLUID VELOCITY, ft./sec.
VELS = GS/(3600.0*SDEN)
CALCULATE THE REYNOLDS NUMBER
RES = (GS*DEQS)/(2.42*VISS)
CALCULATE THE PRANDTL NUMBER
PRS = (CPS*2.42*VISS)/KS
CALCULATE THE FRICTION FACTOR (Dennis Wright: Basic Programs for
chemical engineers, Van Nostrand Reinhold Company, NY 1986.)
703
30
5O
C
C
90
C
CALCULATE THE FRICTION FACTOR
CALL FFACTOR (RES, FRICTS)
CALCULATE THE PRESSURE DROP, psi.
CALL PDROP (FRICTS, TL, NSP, GS, SDEN, DEQS, DROPS)
IF (FLUIDS .EQ. 'LIQUID' .OR. FLUIDS .EQ. 'liquid') THEN
GO TO 3O
ELSEIF (FLUIDS .EQ. 'VAPOR' .OR. FLUIDS .EQ. 'vapor') THEN
CALCULATE THE HEAT TRANSFER FILM COEFFICIENT IN THE VAPOR STATE
HTFS = HTFCV(CPS,GS,DEQS)
ENDIF
GO TO 90
IF (RES .LT. 2100.0) THEN
GO TO 50
ELSE
HTFS = HTFCL (RES,PRS,KS,DEQS)
ENDIF
GO TO 90
HTFS = HTFCJ (RES, PRS, KS, DEQS, TL)
CALCULATE THE HEAT-TRANSFER FILM COEFFICIENT CORRECTED
FOR FOULING.
HIFS = HTFS/(I.0+HTFS*FOLS)
CALCULATE THE OVERALL HEAT TRANSFER COEFFICIENT.
DELTW = (ODT/12.)-(IDT/12.0)
RATIO2 = (DELTW/KST)+(I.0/(HIFTU*RATIOI))+(I.0/HIFS)
UO = 1.0/RATIO2
RETURN
END
PROGRAM CALCULATES HEAT-TRANSFER FILM COEFFICIENT IN THE
SHELL SIDE (FINNED-TUBE) AND THE OVERALL HEAT TRANSFER
COEFFICIENT OF THE HEAT EXCHANGER.
SUBROUTINE PROG3
CHARACTER*30 FLUIDT,FLUIDF,FTSHELL,FTTUBE
REAL IDF,ODF,KF,KFT,KT,NFA,IDT,ODT
704
REAL IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
COMMON/DATA/FTTUBE,
FTSHELL, TDEN, SDEN
COMMON/DATAI/FLUIDT,IDT,ODT,WT,CPT,VIST,KT,TTI,TT2,FOLT,TL,NTP
COMMON/DATA3/FLUIDF,IDF,ODF,WF,CPF,VISF,KF,TFI,TF2,FOLF,
FHT,FTHICK,NF,KFT,NFP
COMMON/DATA4/PI
COMMON/DATA5/IDTF, IDSF, IDFF, ODTF, ODSF, ODFF
COMMON/RES3/VELF,REF,PRF,FRICTF,DROPF,HTFF,HIFF,X,FE,ESEF,HIFD,
UO
IDFF = IDF/12.0
ODFF = ODF/12.0
ODTF = ODT/12.0
AF = (2.0*FHT*FLOAT(NF))/12.0
AO = (PI*ODTF)/12.0+AF
CALCULATE CROSS-SECTIONAL AREA, SHELL SIDE WITHOUT FINS, ft^2.
CSA = (PI*(IDFF**2-ODTF**2))/4.0
CALCULATE NET FREE CROSS-SECTIONAL AREA, SHELL SIDE, ft^2.
NFA = CSA-(FHT*FTHICK*FLOAT(NF))/144.0
CALCULATE THE CROSS-SECTIONAL AREA.
CAF = (PI*IDFF**2)/4.0
CALCULATE THE MASS VELOCITY, ib/ftA2.hr.
GF = WF/NFA
CALCULATE THE FLUID VELOCITY, ft./sec.
VELF = GF/(3600.0*SDEN)
CALCULATE THE WETTED PERIMETER.
DENOM = (PI*(IDFF+ODTF))-(FTHICK*FLOAT(NF))/12.0+AF
DEQF = (4.0*NFA)/DENOM
CALCULATE THE REYNOLDS NUMBER
REF = (GF*DEQF)/(2.42*VISF)
CALCULATE THE PRANDTL NUMBER
PRF = (CPF*2.42*VISF)/KF
CALCULATE THE FRICTION FACTOR
CALL FFACTOR (REF, FRICTF)
CALCULATE THE PRESSURE DROP
CALL PDROP (FRICTF, TL, NFP, GF, SDEN, DEQF, DROPF)
CHECK WHETHER THE FLUID IN THE SHELL SIDE IS LIQUID OR VAPOR.
705
30
50
C
C
90
C
C
IF(FLUIDF .EQ. 'LIQUID' .OR. FLUIDF .EQ. 'liquid') THEN
GO TO 30
ELSEIF (FLUIDF .EQ. 'VAPOR" .OR. FLUIDF .EQ. 'vapor') THEN
CALCULATE THE HEAT-TRANSFER FILM COEFFICIENT IN THE VAPOR STATE.
HTFF = HTFCV (CPF, GF, DEQF)
ENDIF
GO TO 90
IF ( REF .LT. 2100.0) THEN
GO TO 50
ELSE
HTFF = HTFCL (REF, PRF, KF, DEQF)
ENDIF
GO TO 9O
HTFF = HTFCJ (REF, PRF, KF, DEQF, TL)
CALCULATE THE HEAT-TRANSFER FILM COEFFICIENT CORRECTED
FOR FOULING.
HIFF = HTFF/(I.0+HTFF*FOLF)
CALCULATE THE OVERALL HEAT-TRANSFER COEFFICIENT.
CALCULATE THE PARAMETER X, USED IN THE FIN EFFICIENCY
X = FHT*(HIFF/(6.0*KFT*FTHICK))**0.5
CALCULATE THE FIN EFFICIENCY
VALI = EXP(X)-EXP(-X)
VAL2 = EXP(X)+EXP(-X)
FE = (I.0/X*(VALI/VAL2))
CALCULATE
THE EFFECTIVE SURFACE EFFICIENCY FOR FINS
ESEF = FE*(AF/AO)+(I.0-AF/AO)
CALCULATE THE CORRECTED FILM HEAT TRANSFER RATE
HIFD = HIFF*ESEF
CONVERT THE FIN EFFICIENCY AND EFFECTIVE SURFACE EFFICIENCY
TO PERCENTAGES.
FE = 100.0*FE
ESEF = 100.0*ESEF
CALCULATE OVERALL HEAT TRANSFER COEFFICIENT.
DELTW = (ODT/12.0)-(IDT/12.0)
RATIO3 = (PI*IDT)/((PI*ODT)+AF)
RATIO4 = (DELTN/KFT)+(I.0/(HIFF*RATIO3))+(I.0/HIFD)
UO = 1.O/RATIO4
706