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-   -   anyone know the problem of my cavitation flow? (https://www.cfd-online.com/Forums/cfx/91171-anyone-know-problem-my-cavitation-flow.html)

alloveyou August 2, 2011 11:35
anyone know the problem of my cavitation flow?
 
The problem is like that:when i set the saturation pressure as constant in the cavitation,it's fine,but if i set the pressure as the function of temperature ,it always made an error below:

Slave: 2
Slave: 2 Details of error:-
Slave: 2 ----------------
Slave: 2 Error detected by routine MAKDAT
Slave: 2 CDANAM = PSATREL CDTYPE = REAL ISIZE = 903
Slave: 2 CRESLT = OLD
Slave: 2
Slave: 2 Current Directory : /FLOW/PHYSICS/MATERIALS/MT2/ENTHSTAT
.
.
.
+--------------------------------------------------------------------+
| ERROR #001100279 has occurred in subroutine ErrAction. |
| Message: |
| Stopped in routine MEMERR |
| |
| |
| |
| |
| |
+--------------------------------------------------------------------+
anyone know the problem and how to solve it?
Thank you very much!

congtuha August 29, 2011 17:31
Quote:
Originally Posted by alloveyou (Post 318527)
The problem is like that:when i set the saturation pressure as constant in the cavitation,it's fine,but if i set the pressure as the function of temperature ,it always made an error below:

Slave: 2
Slave: 2 Details of error:-
Slave: 2 ----------------
Slave: 2 Error detected by routine MAKDAT
Slave: 2 CDANAM = PSATREL CDTYPE = REAL ISIZE = 903
Slave: 2 CRESLT = OLD
Slave: 2
Slave: 2 Current Directory : /FLOW/PHYSICS/MATERIALS/MT2/ENTHSTAT
.
.
.
+--------------------------------------------------------------------+
| ERROR #001100279 has occurred in subroutine ErrAction. |
| Message: |
| Stopped in routine MEMERR |
| |
| |
| |
| |
| |
+--------------------------------------------------------------------+
anyone know the problem and how to solve it?
Thank you very much!
You should check if the temperature and pressure of your solution are in the range of valid or not. Take a look at the standard for the thermodynamic properties of water over a wide range of temperature and pressure which is provided by the IAPWS Industrial Formulation 1997. The link to download is:
http://www.cheresources.com/content/...ater-and-steam
I have also worked on the compressible cavitating flows. If you want to use my subroutine developed for IAPWS-IF97 just tell me.

ghorrocks August 29, 2011 18:34
Why not use the built-in IAPWS water properties?

congtuha August 30, 2011 00:58
Quote:
Originally Posted by ghorrocks (Post 322144)
Why not use the built-in IAPWS water properties?
Do you think it is a good way to use the built-in in your fortran code? :)

ghorrocks August 30, 2011 06:11
I do not understand your point. The IAPWS water properties are already available in CFX so you do not need to code anything in fortran to get them. It is available through the GUI. But I guess it is good fortran training :)

s3336481 May 15, 2012 00:18
flash boiling flows
 
Quote:
Originally Posted by congtuha (Post 322141)
You should check if the temperature and pressure of your solution are in the range of valid or not. Take a look at the standard for the thermodynamic properties of water over a wide range of temperature and pressure which is provided by the IAPWS Industrial Formulation 1997. The link to download is:
http://www.cheresources.com/content/...ater-and-steam
I have also worked on the compressible cavitating flows. If you want to use my subroutine developed for IAPWS-IF97 just tell me.
Hi congtuha,

I am modelling flash boiling flows in CFX. I wonder if I could have your subroutine developed for IAPWS-IF97?

Thanks in advance :)

ghorrocks May 15, 2012 07:42
Um - did you read my posts? You do not need to code IAPWS-97 as it is already in CFX. If you have time to waste then feel free to code it up but I have better things to do with my time.

s3336481 May 15, 2012 15:55
Quote:
Originally Posted by ghorrocks (Post 361172)
Um - did you read my posts? You do not need to code IAPWS-97 as it is already in CFX. If you have time to waste then feel free to code it up but I have better things to do with my time.
Hi ghorrocks,

Thanks for your comment. I thought the mentioned code in previous posts is modification of IAPWS-IF97 which can model "metastable state" present during the cavitation and flash boiling. So the built-in IAPWS is accurate enough to model "metastable state" ?

ghorrocks May 15, 2012 19:38
The IAPWS-97 model is pretty accurate in the metastable region and this is included in the CFX built in model.

congtuha December 23, 2015 06:16
Quote:
Originally Posted by s3336481 (Post 361092)
Hi congtuha,

I am modelling flash boiling flows in CFX. I wonder if I could have your subroutine developed for IAPWS-IF97?

Thanks in advance :)
Sorry. I have not visited this site for such a long time. Here, I'd give you the subroutines for calculations of water, vapor properties and their derivatives with respect to p and T under thermodynamic equilibrium assumptions:

SUBROUTINE CONSTANT
IMPLICIT NONE
REAL*8 CII1,CJI1,CNI1
REAL*8 CNI2,CNI6,CNI7,CNI9,CNIJ10,CNI11
REAL*8 CJI0,CNI0
REAL*8 CII4,CJI4,CNI4
REAL*8 CII5,CJI5,CNI5
REAL*8 CII8,CJI8,CNI8
COMMON/TAB1/CII1(34),CJI1(34),CNI1(34),CNI2(5),CJI0(9),CNI0(9) ,
& CII4(43),CJI4(43),CNI4(43),CII5(40),CJI5(40),CNI5( 40),
& CNI6(10),CNI7(4),CII8(19),CJI8(19),CNI8(19),CNI9(4 ),
& CNIJ10(6,5),CNI11(5)
INTEGER I

REAL*8 INDE(43)
OPEN(111,FILE='TABLES.DAT')
DO I=1,15
READ(111,*)
ENDDO
DO I=1,34
READ(111,*)INDE(I),CII1(I),CJI1(I),CNI1(I)
ENDDO
C READ TABLE 2
READ(111,*)
READ(111,*)
DO I=1,5
READ(111,*)INDE(I),CNI2(I)
ENDDO
C READ TABLE 3
READ(111,*)
READ(111,*)
DO I=1,9
READ(111,*)INDE(I),CJI0(I),CNI0(I)
ENDDO
C READ TABLE 4
READ(111,*)
READ(111,*)
DO I=1,43
READ(111,*)INDE(I),CII4(I),CJI4(I),CNI4(I)
ENDDO
C READ TABLE 5
READ(111,*)
READ(111,*)
DO I=1,40
READ(111,*)INDE(I),CII5(I),CJI5(I),CNI5(I)
ENDDO

C READ TABLE 6
READ(111,*)
READ(111,*)
DO I=1,10
READ(111,*)INDE(I),CNI6(I)
ENDDO
C READ TABLE 7
READ(111,*)
READ(111,*)
DO I=1,4
READ(111,*)INDE(I),CNI7(I)
ENDDO
C READ TABLE 8
READ(111,*)
READ(111,*)
DO I=1,19
READ(111,*)INDE(I),CII8(I),CJI8(I),CNI8(I)
ENDDO

C READ TABLE 9
READ(111,*)
READ(111,*)
DO I=1,4
READ(111,*)INDE(I),CNI9(I)
ENDDO
C READ TABLE 11
READ(111,*)
READ(111,*)
DO I=1,5
READ(111,*)INDE(I),CNI11(I)
ENDDO
C READ TABLE 10
READ(111,*)
READ(111,*)
DO I=1,6
READ(111,*)CNIJ10(I,1),CNIJ10(I,2),CNIJ10(I,3),CNI J10(I,4),CNIJ10(I,5)
ENDDO
CLOSE(111)
RETURN
END

SUBROUTINE PROP(YV,TNK,PPASL,PV,DROLP,DROLT,DHLP,DHLT,HLP,
& ROLP,DROVP,DROVT,DHVP,DHVT,HVP,ROVP,PSATP,TSATP,IF L,
& MULP,MUVP,CKLP,CKVP)
IMPLICIT NONE
REAL*8 CII1,CJI1,CNI1
REAL*8 CNI2,CNI6,CNI7,CNI9,CNIJ10,CNI11
REAL*8 CJI0,CNI0
REAL*8 CII4,CJI4,CNI4
REAL*8 CII5,CJI5,CNI5
REAL*8 CII8,CJI8,CNI8
COMMON/TAB1/CII1(34),CJI1(34),CNI1(34),CNI2(5),CJI0(9),CNI0(9) ,
& CII4(43),CJI4(43),CNI4(43),CII5(40),CJI5(40),CNI5( 40),
& CNI6(10),CNI7(4),CII8(19),CJI8(19),CNI8(19),CNI9(4 ),
& CNIJ10(6,5),CNI11(5)
REAL*8 TLIM1,TLIM2,TLIM3,TLIM4,TLIM5,R

PARAMETER (TLIM1=273.15D0,TLIM2=623.15D0,TLIM3=647.096D0)
PARAMETER (TLIM4=863.15D0,TLIM5=1073.15,R=461.526D0)
INTEGER II,IFL
REAL*8 DROLP,DROLT,DHLP,DHLT,HLP,ROLP,MULP,MUVP,CKLP,CKVP
REAL*8 DROVP,DROVT,DHVP,DHVT,HVP,ROVP,PSATP,PB23
REAL*8 PPASL,PPASV,TNK,TNKL,TNKV,TAUL,TAUV,TS,AAS,BBS,CCS ,PAIL,PAIV,
& GPI,GPIPI,GPITAU,GTAU,GTAUTAU,GTAUPI,GPIR,
& GPIPI0,GPIPIR,GPITAU1R,GTAU1R,GTAU1PI0,
& GTAU1PIR,GTTR,GTAU10,GTT0,YV,THETA
REAL*8 PP,BET,EES,FFS,GGS,DDS,TSATP,PV
PP=PPASL
PPASV=PPASL
TS=TNK;TNKL=TNK;TNKV=TNK
C COMPUTE SATURATION TEMPERATURE
C CHECK IF P IS OUTSITE THE VALID RANGE FOR REGION...
IF (PP.LT.611.212677D0)PP=611.212677D0
IF (PP.GT.22.064D6)PP=22.064D6
BET=(PP/1.D6)**0.25D0
EES=BET**2.D0+CNI6(3)*BET+CNI6(6)
FFS=CNI6(1)*BET**2.D0+CNI6(4)*BET+CNI6(7)
GGS=CNI6(2)*BET**2.D0+CNI6(5)*BET+CNI6(8)
DDS=2.D0*GGS/(-FFS-DSQRT(FFS**2.D0-4.D0*EES*GGS))
TSATP=0.5D0*(CNI6(10)+DDS-
& DSQRT( (CNI6(10)+DDS)**2.D0 -4.D0*(CNI6(9)+CNI6(10)*DDS) ) )
C COMPUTE SATURATION PRESSURE
C CHECK IF TS IS OUTSITE THE VALID RANGE FOR REGION 4
IF (TS.LT.TLIM1)TS=TLIM1
IF (TS.GT.TLIM2)TS=TLIM2
THETA=TS+CNI6(9)/(TS-CNI6(10))
AAS=THETA**2.D0+CNI6(1)*THETA+CNI6(2)
BBS=CNI6(3)*THETA**2.D0+CNI6(4)*THETA+CNI6(5)
CCS=CNI6(6)*THETA**2.D0+CNI6(7)*THETA+CNI6(8)
PSATP=1.0D+06*(2.D0*CCS/
1 (-BBS+DSQRT(BBS**2.D0-4.D0*AAS*CCS)))**4.D0

C COMPUTE BOILING PRESSURE
PB23=1.D6*(CNI11(1)+CNI11(2)*TNK+CNI11(3)*TNK**2.D 0)
C COMPUTE LIQUID AND VAPOR DENSITY
C CHECK IF TNKL AND PPASL ARE OUTSITE THE VALID RANGE FOR REGION 1
IF (TNKL.LT.TLIM1)TNKL=TLIM1
IF (TNKL.GT.TLIM2)TNKL=TLIM2

IF (PPASL.LT.PSATP)PPASL=PSATP
IF (PPASL.GT.1.0D8)PPASL=1.0D8

IF (YV.NE.0.D0) PPASL=PSATP
C CHECK IF TNKV AND PPASV ARE OUTSITE THE VALID RANGE FOR REGION 2
IF (TNKV.LT.TLIM1)TNKV=TLIM1
IF (TNKV.GT.TLIM5)TNKV=TLIM5
IF (YV.NE.1.D0.OR.PPASV.GT.PSATP)PPASV=PSATP
IF (TNKV.GT.TLIM2.AND.TNKV.LE.TLIM4.AND.PPASV.GT.PB23 )PPASV=PB23
IF (TNKV.GT.TLIM4.AND.TNKV.LE.TLIM5.AND.PPASV.GT.1.D8 )PPASV=1.D8
IF (PPASV.LT.611.212677D0) PPASV=611.212677D0

PAIL=PPASL/16.53D+06
PAIV=PPASV/1.0D+06
TAUL=1386.0D0/TNKL
TAUV=540.0D0/TNKV

C PARAMETERS FOR LIQUID
GPI =0.D0
GPIPI =0.D0
GPITAU =0.D0
GTAU =0.D0
GTAUTAU=0.D0
GTAUPI =0.D0
C PARAMETERS FOR VAPOR
GPIR =0.D0
GPIPI0 =-1.D0/PAIV**2.D0
GPIPIR =0.D0
GPITAU1R=0.D0
GTAU1R =0.D0
GTAU1PI0=0.D0
GTAU1PIR=0.D0
GTTR =0.D0
GTAU10 =0.D0
GTT0 =0.D0
DO II=1,43
IF (II.LE.34)THEN
C COMPUTE LIQUID DENSITY
GPI =GPI-CNI1(II)*CII1(II)*(7.1D0-PAIL)**(CII1(II)-1.D0)
& *(TAUL-1.222D0)**CJI1(II)
C COMPUTE DERIVATIVES OF LIQUID DENSITY WITH RESPECT TO P AND T
GPIPI =GPIPI+CNI1(II)*CII1(II)*(CII1(II)-1.D0)*(7.1D0-PAIL)**
& (CII1(II)-2.D0)*(TAUL-1.222D0)**CJI1(II)
GPITAU=GPITAU-CNI1(II)*CII1(II)*(7.1D0-PAIL)**(CII1(II)-1.D0)*
& CJI1(II)*(TAUL-1.222D0)**(CJI1(II)-1.D0)
C COMPUTE LIQUID ENTHALPY
GTAU =GTAU+CNI1(II)*(7.1D0-PAIL)**CII1(II)*
& CJI1(II)*(TAUL-1.222D0)**(CJI1(II)-1.D0)
C COMPUTE THE DERIVATIVES OF LIQUID ENTHALPY WITH RESPECT TO P AND T
GTAUTAU=GTAUTAU+CNI1(II)*(7.1D0-PAIL)**CII1(II)*CJI1(II)*
& (CJI1(II)-1.D0)*(TAUL-1.222D0)**(CJI1(II)-2.D0)

GTAUPI =GTAUPI-CNI1(II)*CII1(II)*(7.1D0-PAIL)**(CII1(II)-1.D0)*
& CJI1(II)*(TAUL-1.222D0)**(CJI1(II)-1.D0)
ENDIF !II<=34
IF (II.LE.9)THEN
GTAU10 =GTAU10+CNI0(II)*CJI0(II)*TAUV**(CJI0(II)-1.D0)
GTT0 =GTT0+CNI0(II)*CJI0(II)*(CJI0(II)-1.D0)*
& TAUV**(CJI0(II)-2.D0)
ENDIF !II<=9
GPIR =GPIR+CNI4(II)*CII4(II)*
& PAIV**(CII4(II)-1.D0)*(TAUV-0.5D0)**CJI4(II)
COMPUTE DERIVATIVES OF VAPOR DENSITY WITH RESPECTO P AND T
GPIPIR =GPIPIR +CNI4(II)*CII4(II)*(CII4(II)-1.D0)*
& PAIV**(CII4(II)-2.D0)*(TAUV-0.5D0)**CJI4(II)
GPITAU1R=GPITAU1R +CNI4(II)*CII4(II)*PAIV**(CII4(II)-1.D0)*
& CJI4(II)*(TAUV-0.5D0)**(CJI4(II)-1.D0)
GTAU1R=GTAU1R+CNI4(II)*PAIV**CII4(II)*
& CJI4(II)*(TAUV-0.5D0)**(CJI4(II)-1.D0)
C COMPUTE DERIVATIVES OD VAPOR ENTHALPY ABOUT P AND T : CPSATVAPTW(T)
GTAU1PIR=GTAU1PIR+CNI4(II)*CII4(II)*PAIV**(CII4(II )-1.D0)*
& CJI4(II)*(TAUV-0.5D0)**(CJI4(II)-1.D0) !!
GTTR=GTTR+CNI4(II)*PAIV**CII4(II)*CJI4(II)*
& (CJI4(II)-1.D0)*(TAUV-0.5D0)**(CJI4(II)-2.D0)
ENDDO

DROLP=-GPIPI/R/TNKL/GPI**2.D0
DROLT=-16.53D+06*(GPI-TAUL*GPITAU)/R/TNKL**2.D0/GPI**2.D0
DHLT=-TAUL**2.D0*R*GTAUTAU
DHLP=1386.0D0*R*GTAUPI/16.53D+06
ROLP=(R*TNKL*GPI/16.53D+06)**(-1.D0)
HLP=R*1386.0D0*GTAU

DROVP=-(GPIPI0+GPIPIR)/R/TNKV/(1.D0/PAIv+GPIR)**2.D0
DROVT=-1.0D+6/R/TNKV**2.D0*(1.D0/
1 (1.D0/PAIV+GPIR)-TAUV*GPITAU1R/(1.D0/PAIV+GPIR)**2.D0)
DHVP=R*540.D0/1.0D+06*(GTAU1PI0+GTAU1PIR)
DHVT=-R*TAUV**2.D0*(GTT0+GTTR)
ROVP=(R*TNKV/1.0D+06*(1.D0/PAIV+GPIR))**(-1.D0)
HVP=R*540.D0*(GTAU10+GTAU1R)
IF (IFL.EQ.1)CALL VISCOSITY(TNKL,TNKV,PPASL,PPASV,ROLP,ROVP,
& MULP,MUVP,CKLP,CKVP)
PPASL=PP; PV=PPASV
RETURN
END
SUBROUTINE VISCOSITY(TNKL,TNKV,PPASL,PPASV,ROLP,ROVP,
& MULP,MUVP,CKLP,CKVP)
IMPLICIT NONE
REAL*8 CII1,CJI1,CNI1
REAL*8 CNI2,CNI6,CNI7,CNI9,CNIJ10,CNI11
REAL*8 CJI0,CNI0
REAL*8 CII4,CJI4,CNI4
REAL*8 CII5,CJI5,CNI5
REAL*8 CII8,CJI8,CNI8
COMMON/TAB1/CII1(34),CJI1(34),CNI1(34),CNI2(5),CJI0(9),CNI0(9) ,
& CII4(43),CJI4(43),CNI4(43),CII5(40),CJI5(40),CNI5( 40),
& CNI6(10),CNI7(4),CII8(19),CJI8(19),CNI8(19),CNI9(4 ),
& CNIJ10(6,5),CNI11(5)

REAL*8 TNKL,TNKV,TNK,TNC,PPASL,PPASV,ROLP,ROVP,MULP,MUVP, MU0L,MU1L,
& MU0V,MU1V,DL,DV,TAUL,TAUV,SUML,SUMV,CKLP,CKVP,CK0L ,CK1L,
& CK0V,CK1V
INTEGER I
REAL*8 DV1,DV2,DV3,DV4,DV11,DV21,DV31,DV41

DV1= 0.15541443D+01
DV2= 0.66106305D+02
DV3= 0.55969886D+04
DV4= -0.39259598D+01
DV11= 0.79349503D+00
DV21=-0.13340063D+04
DV31= 0.37884327D+06
DV41= 0.23591474D+01

TNK=TNKL
DL=ROLP/317.763D0
DV=ROVP/317.763D0
TAUL=647.226D0/TNKL
TAUV=647.226D0/TNKV
C VISCOSITY
SUML=0.D0
SUMV=0.D0

DO I=1,4
SUML=SUML+CNI7(I)*TAUL**(I-1)
SUMV=SUMV+CNI7(I)*TAUV**(I-1)
ENDDO
MU0L=1.D0/(DSQRT(TAUL)*SUML)
MU0V=1.D0/(DSQRT(TAUV)*SUMV)

SUML=0.D0
SUMV=0.D0
DO I=1,19
SUML=SUML+CNI8(I)*(DL-1.D0)**CII8(I)*(TAUL-1.D0)**CJI8(I)
SUMV=SUMV+CNI8(I)*(DV-1.D0)**CII8(I)*(TAUV-1.D0)**CJI8(I)
ENDDO
MU1L=DEXP(DL*SUML)
MU1V=DEXP(DV*SUMV)

MULP=55.071D-6*MU0L*MU1L
MUVP=55.071D-6*MU0V*MU1V
C THERMALCONDUCTIVITY
C COMPUTE THE THERMAL CONDUCTIVITY OF LIQUID, VAPOR
IF (TNK.LT.1000.D0)THEN
CKVP=1.0D-04*DEXP(DV1*DLOG(TNK)+DV2/TNK+DV3/TNK**2.D0+DV4) ! W/M.K
ELSE
CKVP=1.0D-04*DEXP(DV11*DLOG(TNK)+DV21/TNK+DV31/TNK**2.D0+DV41) ! W/M.K
ENDIF

IF (TNK.GT.347.15) TNK=347.15
TNC=TNK-273.15D0
CKLP =0.56075D0+1.9947D-03*TNC-7.9003D-06*TNC**2.D0 ! W/M.K
RETURN
END

TABLES.DAT
** DATA FOR THERMODYNAMIC CALCUATIONS OF VAPOR AND LIQUID**
** TABLE 1 FOR CALUCALTIONS OF : LIQUID DENSITY, LIQUID ENTHALPY AND THE DERIVATIVES OF LIQUID DENSITY AND ENTHALPY WITH RESPEC TO P AND T
** TABLE 2 FOR CALUCALTIONS OF BOILING PRESSURE
** TABLE 3-4 FOR CALUCALTIONS OF : VAPOR DENSITY, VAPOR ENTHALPY AND THE DERIVATIVES OF LIQUID DENSITY AND ENTHALPY WITH RESPEC TO P AND T
IN SATURATION REGION (REGION 2)
** TABLE 5 FOR CALUCALTIONS OF : VAPOR DENSITY, VAPOR ENTHALPY AND THE DERIVATIVES OF LIQUID DENSITY AND ENTHALPY WITH RESPEC TO P AND T
IN BOIING REGION (REGION 3)
** TABLE 6 FOR CALUCALTIONS OF SATURATION PRESSURE
** TABLE 7 FOR CALUCALTIONS OF DYNAMIC VISCOSITY OF VAPOR
** TABLE 8 FOR CALUCALTIONS OF DYNAMIC VISCOSITY OF LIQUID
** TABLE 9 FOR CALUCALTIONS OF THERMAL CONDUCTIVITY OF VAPOR
** TABLE 10 FOR CALUCALTIONS OF THERMAL CONDUCTIVITY OF LIQUID

Table1:Coefficients ande xponents of the fundamental equation and itsderivatives
i Ii Ji ni
1 0 -2 0.14632971213167E+00
2 0 -1 -0.84548187169114E+00
3 0 0 -0.37563603672040E+01
4 0 1 0.33855169168385E+01
5 0 2 -0.95791963387872E+00
6 0 3 0.15772038513228E+00
7 0 4 -0.16616417199501E-01
8 0 5 0.81214629983568E-03
9 1 -9 0.28319080123804E-03
10 1 -7 -0.60706301565874E-03
11 1 -1 -0.18990068218419E-01
12 1 0 -0.32529748770505E-01
13 1 1 -0.21841717175414E-01
14 1 3 -0.52838357969930E-04
15 2 -3 -0.47184321073267E-03
16 2 0 -0.30001780793026E-03
17 2 1 0.47661393906987E-04
18 2 3 -0.44141845330846E-05
19 2 17 -0.72694996297594E-15
20 3 -4 -0.31679644845054E-04
21 3 0 -0.28270797985312E-05
22 3 6 -0.85205128120103E-09
23 4 -5 -0.22425281908000E-05
24 4 -2 -0.65171222895601E-06
25 4 10 -0.14341729937924E-12
26 5 -8 -0.40516996860117E-06
27 8 -11 -0.12734301741641E-08
28 8 -6 -0.17424871230634E-09
29 21 -29 -0.68762131295531E-18
30 23 -31 0.14478307828521E-19
31 29 -38 0.26335781662795E-22
32 30 -39 -0.11947622640071E-22
33 31 -40 0.18228094581404E-23
34 32 -41 -0.93537087292458E-25
Table 2.
i ni
1 0.34805185628969E+03
2 -0.11671859879975E+01
3 0.10192970039326E-02
4 0.57254459862746E+03
5 0.13918839778870E+02
Table.3.Coefficientsandexponentsoftheideal-gaspartofthefundamentalequationanditsderivatives
i Ji0 ni0
1 0 -0.96927686500217E+01
2 1 0.10086655968018E+02
3 -5 -0.56087911283020E-02
4 -4 0.71452738081455E-01
5 -3 -0.40710498223928E+00
6 -2 0.14240819171444E+01
7 -1 -0.43839511319450E+01
8 2 -0.28408632460772E+00
9 3 0.21268463753307E-01
Table4.Coefficientsandexponentsoftheresidualpartof thefundamentalequationanditsderivatives
i Ii Ji ni
1. 1. 0. -0.17731742473213E-02
2 1. 1. -0.17834862292358E-01
3 1 2 -0.45996013696365E-01
4 1 3 -0.57581259083432E-01
5 1 6 -0.50325278727930E-01
6 2 1 -0.33032641670203E-04
7 2 2 -0.18948987516315E-03
8 2 4 -0.39392777243355E-02
9 2 7 -0.43797295650573E-01
10 2 36 -0.26674547914087E-04
11 3 0 0.20481737692309E-07
12 3 1 0.43870667284435E-06
13 3 3 -0.32277677238570E-04
14 3 6 -0.15033924542148E-02
15 3 35 -0.40668253562649E-01
16 4 1 -0.78847309559367E-09
17 4 2 0.12790717852285E-07
18 4 3 0.48225372718507E-06
19 5 7 0.22922076337661E-05
20 6 3 -0.16714766451061E-10
21 6 16 -0.21171472321355E-02
22 6 35 -0.23895741934104E+02
23 7 0 -0.59059564324270E-17
24 7 11 -0.12621808899101E-05
25 7 25 -0.38946842435739E-01
26 8 8 0.11256211360459E-10
27 8 36 -0.82311340897998E+01
28 9 13 0.19809712802088E-07
29 10 4 0.10406965210174E-18
30 10 10 -0.10234747095929E-12
31 10 14 -0.10018179379511E-08
32 16 29 -0.80882908646985E-10
33 16 50 0.10693031879409E+00
34 18 57 -0.33662250574171E+00
35 20 20 0.89185845355421E-24
36 20 35 0.30629316876232E-12
37 20 48 -0.42002467698208E-05
38 21 21 -0.59056029685639E-25
39 22 53 0.37826947613457E-05
40 23 39 -0.12768608934681E-14
41 24 26 0.73087610595061E-28
42 24 40 0.55414715350778E-16
43 24 58 -0.94369707241210E-06
Table 5: Coefficients and exponents of the fundamental equation and its derivatives (REGION3)
i Ii Ji ni
1 0 0 0.10658070028513E+01
2 0 0 -0.15732845290239E+02
3 0 1 0.20944396974307E+02
4 0 2 -0.76867707878716E+01
5 0 7 0.26185947787954E+01
6 0 10 -0.28080781148620E+01
7 0 12 0.12053369696517E+01
8 0 23 -0.84566812812502E-02
9 1 2 -0.12654315477714E+01
10 1 6 -0.11524407806681E+01
11 1 15 0.88521043984318E+00
12 1 17 -0.64207765181607E+00
13 2 0 0.38493460186671E+00
14 2 2 -0.85214708824206E+00
15 2 6 0.48972281541877E+01
16 2 7 -0.30502617256965E+01
17 2 22 0.39420536879154E-01
18 2 26 0.12558408424308E+00
19 3 0 -0.27999329698710E+00
20 3 2 0.13899799569460E+01
21 3 4 -0.20189915023570E+01
22 3 16 -0.82147637173963E-02
23 3 26 -0.47596035734923E+00
24 4 0 0.43984074473500E-01
25 4 2 -0.44476435428739E+00
26 4 4 0.90572070719733E+00
27 4 26 0.70522450087967E+00
28 5 1 0.10770512626332E+00
29 5 3 -0.32913623258954E+00
30 5 26 -0.50871062041158E+00
31 6 0 -0.22175400873096E-01
32 6 2 0.94260751665092E-01
33 6 26 0.16436278447961E+00
34 7 2 -0.13503372241348E-01
35 8 26 -0.14834345352472E-01
36 9 2 0.57922953628084E-03
37 9 26 0.32308904703711E-02
38 10 0 0.80964802996215E-04
39 10 1 -0.16557679795037E-03
40 11 26 -0.44923899061815E-04
Table 6: Coefficients of the saturation pressure and temperature equations
i ni
1 0.11670521452767E+04
2 -0.72421316703206E+06
3 -0.17073846940092E+02
4 0.12020824702470E+05
5 -0.32325550322333E+07
6 0.14915108613530E+02
7 -0.48232657361591E+04
8 0.40511340542057E+06
9 -0.23855557567849E+00
10 0.65017534844798E+03
Table 7: Coefficients of the ideal gas part -(Dynamic Viscosity OF VAPOR)
i ni
0 0.100000E+01
1 0.978197
2 0.579829
3 -0.202354
Table 8: Coefficients and exponents of the real fluid part-Dynamic Viscosity
i Ii Ji ni
1 0 0 0.5132047
2 0 1 0.3205656
3 0 4 -0.7782567
4 0 5 0.1885447
5 1 0 0.2151778
6 1 1 0.7317883
7 1 2 0.1241044E+01
8 1 3 0.1476783E+01
9 2 0 -0.2818107
10 2 1 -0.1070786E+01
11 2 2 -0.1263184E+01
12 3 0 0.1778064
13 3 1 0.4605040
14 3 2 0.2340379
15 3 3 -0.4924179
16 4 0 -0.4176610E-01
17 4 3 0.1600435
18 5 1 -0.1578386E-01
19 6 3 -0.3629481E-02
Table 9: Coefficients of the ideal gas part-Thermal Conductivity
i ni
0 0.1000000E+01
1 0.6978267E+01
2 0.2599096E+01
3 -0.9982540
Table 11: Coefficients of the equations pb23
i ni
1 0.34805185629869D3
2 -0.11671859879975D1
3 0.10192970039326D-2
4 0.57254459862746D3
5 0.13918839778870D2
Table 10: Coefficients nij of the first real fluid part-Thermal Conductivity
i: horizontal; j:vertical
0.13293046E+01 0.17018363E+01 0.52246158E+01 0.87127675E+01 -0.18525999E+01
-0.40452437E+00 -0.22156845E+01 -0.10124111E+02 -0.95000611E+01 0.93404690E+00
0.24409490E+00 0.16511057E+01 0.49874687E+01 0.43786606E+01 0.E+00
0.18660751E-01 -0.76736002E+00 -0.27297694E+00 -0.91783782E+00 0.E+00
-0.12961068E+00 0.37283344E+00 -0.43083393E+00 0.E+00 0.E+00
0.44809953E-01 -0.11203160E+00 0.13333849E+00 0.E+00 0.E+00
Table2.31:
i Ii Ji ni
1 0 0 -0.23872489924521D3
2 0 1 0.40421188637945D3
3 0 2 0.11349746881718D3
4 0 6 -0.58457616048039D1
5 0 22 -0.15285482413140D-3
6 0 32 -0.10866707695377D-5
7 1 0 -0.13391744872602D2
8 1 1 0.43211039183559D2
9 1 2 -0.54010067170506D2
10 1 3 0.30535892203916D2
11 1 4 -0.65964749423638D1
12 1 10 0.93965400878363D-2
13 1 32 0.11573647505340D-6
14 2 10 -0.25858641282073D-4
15 2 32 -0.40644363084799D-8
16 3 10 0.66456186191635D-7
17 3 32 0.80670734103027D-10
18 4 32 -0.93477771213947D-12
19 5 32 0.58265442020601D-14
20 6 32 -0.15020185953503D-16

Hope this helps..!


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