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一些优化：CAN和PLC地址的优化

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R141b !Short name
1717-00-6 !CAS number
1,1-Dichloro-1-fluoroethane !Full name
CCl2FCH3 !Chemical formula {C2H3Cl2F}
HCFC-141b !Synonym
116.94962 !Molar mass [g/mol]
169.68 !Triple point temperature [K]
305.20 !Normal boiling point [K]
477.5 !Critical temperature [K]
4212.0 !Critical pressure [kPa]
3.921 !Critical density [mol/L]
0.2195 !Acentric factor
2.014 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Chem. Eng. Data 36:409-413.
IIR !Default reference state
10.0 !Version number
???? !UN Number :UN:
halocb !Family :Family:
???? !Heating value (upper) [kJ/mol] :Heat:
725. !GWP (IPCC 2007) :GWP:
0.12 !ODP (WMO 2010) :ODP:
2600. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
1S/C2H3Cl2F/c1-2(3,4)5/h1H3 !Standard InChI String :InChi:
FRCHKSNAZZFGCA-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
???? !Alternative fluid for mixing rules :AltID:
ba322c10 !Hash number from InChI Key :Hash:
!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
! end of the fluid file is marked with @END. Anything below that is ignored.
! compiled by E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
! 06-12-97 EWL, Original version.
! 04-12-01 EWL, Add Lemmon and Span short EOS.
! 05-21-02 MLH, Add ECS fits for viscosity, thermal conductivity; changed ref fluid to propane for transport to allow low T calculations.
! 03-13-03 EWL, Replace cp0 equation.
! 01-26-04 EWL, Add final coefficients to EOS.
! 04-19-04 MLH, Update transport references.
! 05-26-04 EWL, Change triple point temperature.
! 08-17-10 IDC, Add ancillary equations.
! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
________________________________________________________________________________
#EOS !---Equation of state---
FEQ !Helmholtz equation of state for R-141b of Lemmon and Span (2006).
:TRUECRITICALPOINT: 477.5 3.921 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
:DOI: 10.1021/je050186n
?
?```````````````````````````````````````````````````````````````````````````````
?Lemmon, E.W. and Span, R.,
? "Short Fundamental Equations of State for 20 Industrial Fluids,"
? J. Chem. Eng. Data, 51(3):785-850, 2006. doi: 10.1021/je050186n
?
?The uncertainties are 0.2% in density between 180 and 400 K at
? pressures to 100 MPa, and 0.5% in density at higher pressures. The
? uncertainty in density may be higher as temperatures approach 400 K. Vapor
? pressures are represented with an uncertainty of 0.2% from 270 to 400 K.
? The uncertainty in speed of sound is 0.01% in the vapor phase and 0.5% in
? the liquid phase. Heat capacity data are not available to verify the equation
? of state, however, the uncertainties are estimated to be within 5 %.
?
!```````````````````````````````````````````````````````````````````````````````
169.68 !Lower temperature limit [K]
500.0 !Upper temperature limit [K]
400000.0 !Upper pressure limit [kPa]
12.56 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
116.94962 !Molar mass [g/mol]
169.68 !Triple point temperature [K]
0.006492 !Pressure at triple point [kPa]
12.56 !Density at triple point [mol/L]
305.20 !Normal boiling point temperature [K]
0.2195 !Acentric factor
477.5 4212.0 3.921 !Tc [K], pc [kPa], rhoc [mol/L]
477.5 3.921 !Reducing parameters [K, mol/L]
8.314472 !Gas constant [J/mol-K]
12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
1.1469 0.25 1. 0. !a(i),t(i),d(i),l(i)
-3.6799 1.25 1. 0.
1.3469 1.5 1. 0.
0.083329 0.25 3. 0.
0.00025137 0.875 7. 0.
0.32720 2.375 1. 1.
0.46946 2.0 2. 1.
-0.029829 2.125 5. 1.
-0.31621 3.5 1. 2.
-0.026219 6.5 1. 2.
-0.078043 4.75 4. 2.
-0.020498 12.5 2. 3.
#AUX !---Auxiliary function for Cp0
CPP !Ideal gas heat capacity function for R-141b of Lemmon and Span (2006).
?
?```````````````````````````````````````````````````````````````````````````````
?Lemmon, E.W. and Span, R., 2006.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 8.314472 !Reducing parameters for T, Cp0
1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
4.0 0.0
6.8978 502.0
7.8157 1571.0
3.2039 4603.0
#AUX !---Auxiliary function for PX0
PX0 !Helmholtz energy ideal-gas function for R-141b of Lemmon and Span (2006).
?
?```````````````````````````````````````````````````````````````````````````````
?Lemmon, E.W. and Span, R., 2006.
?
!```````````````````````````````````````````````````````````````````````````````
1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
-15.5075021375220103 0.0 !aj, ti for [ai*tau**ti] terms
9.187194537955337 1.0 !aj, ti for [ai*tau**ti] terms
6.8978 502.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
7.8157 1571.0
3.2039 4603.0
#AUX !---Auxiliary function for PH0
PH0 !Ideal gas Helmholtz form for R-141b.
?
?```````````````````````````````````````````````````````````````````````````````
?Lemmon, E.W. and Span, R., 2006.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
-15.5074814985 0.0 !aj, ti for [ai*tau**ti] terms
9.1871858933 1.0
6.8978 -1.0513089005 !aj, ti for [ai*log(1-exp(ti*tau)] terms
7.8157 -3.290052356
3.2039 -9.6397905759
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
#TRN !---ECS Transport---
ECS !Extended Corresponding States model (Propane reference); fitted to data for R-141b. (unpublished)
:DOI: 10.1021/ie0300880
?
?```````````````````````````````````````````````````````````````````````````````
?Unpublished; uses method described in the following reference:
?Huber, M.L., Laesecke, A., and Perkins, R.A.,
? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
? a New Correlation for the Viscosity of R134a,"
? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
?
?THERMAL CONDUCTIVITY
? The ECS parameters for thermal conductivity were based in part on the data of:
? Perkins, R., Cusco, L., Howley, J., Laesecke, A., Matthes, S., and Ramires, M.L.V., "Thermal Conductivities of Alternatives to CFC-11 for Foam Insulation," J. Chem. Eng. Data, 46(2):428-432, 2001. doi: 10.1021/je990337k
? Yamamoto, R., Matsuo, S., and Tanaka, Y., "Thermal Conductivity of Halogenated Ethanes, HFC-134a, HCFC-123, and HCFC-141b," Int. J. Thermophys, 14(1):79-90, 1993. doi: 10.1007/BF00522663
? Papadaki, M., Schmitt, M., Seitz, A., Stephan, K., Taxis, B., and Wakeham, W.A., "Thermal Conductivity of R134a and R141b Within the Temperature Range 240-307 K at the Saturation Vapor Pressure," Int. J. Thermophys., 14(2):173-181, 1993. doi: 10.1007/BF00507806
? Yata, J., Hori, M., Kurahashi, T., and Minamiyama, T., "Thermal Conductivity of Alternative Fluorocarbons in Liquid Phase," Fluid Phase Equilib., 80:287-296, 1992.
? Gao, X., Yamada, T., Nagasaka, Y., and Nagashima, A., "The Thermal Conductivity of CFC Alternatives HFC-125 and HCFC-141b in the Liquid Phase," Int. J. Thermophys., 17(2):279-293, 1996.
? Dohrn, R., Treckmann, R., and Heinemann, T., "Vapor-Phase Thermal Conductivity of 1,1,1,2,2-Pentafluoropropane, 1,1,1,3,3-Pentafluoropropane, 1,1,2,2,3- Pentafluoropropane and Carbon Dioxide," Fluid Phase Equilib., 158-160:1021-1028, 1999. doi: 10.1016/S0378-3812(99)00126-0
? Richard, R.G. and Shankland, I.R., "A Transient Hot-Wire Method for Measuring the Thermal Conductivity of Gases and Liquids," Int. J. Thermophys., 10(3):673-686, 1989.
? Tanaka, Y., Nakata, M., and Makita, T., "Thermal Conductivity of Gaseous HFC-134a, HFC-143a, HCFC-141b, and HCFC-142b," Int. J. Thermophys., 12(6):949-963, 1991. doi: 10.1007/BF00503512
? Assael, M.J. and Karagiannidis, L., "Measurements of the Thermal Conductivity of Liquid R32, R124, R125, and R141b," Int. J. Thermophys., 16(4):851-865, 1995.
? Gurova, A.N., Nieto de Castro, C., and Mardolcar, U., "The Thermal Conductivity of Liquid Halocarbons," paper C1c5, Proc. 4th Asian Thermophysical Properties Conf., Tokyo, Japan, 1995.
? Average absolute deviations of the fit from the experimental data are:
? Perkins: 4.42%; Yamamoto: 5.61%; Papadaki 3.16%; Yata: 4.26%; Gao: 0.32%;
? Dohrn: 1.52%; Richard: 1.79%, Tanaka: 16.03%; Assael: 0.27%; Gurova: 3.95%.
? Overall: 3.22%.
?
?VISCOSITY
? The ECS parameters for viscosity were based in part on the data of:
? Diller, D.E., Aragon, A.S., and Laesecke, A., "Measurements of the Viscosities of Saturated and Compressed Liquid 1,1,1,2-Tetrafluoroethane (R134a), 2.2-Dichloro-1,1,1-Trichloroethane (R123) and 1,1-Dichloro-1-Fluoroethane (R141b)," Fluid Phase Equilib., 88:251-162, 1993. doi: 10.1016/0140-7007(93)90016-2
? Kumagai, A. and Yokoyama, C., "Revised Viscosities of Saturated Liquid Halocarbon Refrigerants from 273 to 353 K," Int. J. Thermophys., 21(4):909-912, 2001. doi: 10.1023/A:1006666308831
? Assael, M.J., Polimatidou, S.K., Vogel, E., and Wakeham, W.A., "Measurements of the Viscosity of R11, R12, R141b, and R152a in the Temperature Range 270 - 340 K at Pressures up to 20 MPa," Int. J. Thermophys., 15(4):575-589, 1994.
? Average absolute deviations of the fit from the experimental data are:
? Diller: 2.60%; Kumagai: 1.03%; Assael: 1.80%.
? Overall: 2.12%.
?
?The Lennard-Jones parameters were estimated.
?
!```````````````````````````````````````````````````````````````````````````````
169.68 !Lower temperature limit [K]
500.0 !Upper temperature limit [K]
400000.0 !Upper pressure limit [kPa]
12.56 !Maximum density [mol/L]
FEQ PROPANE.FLD
VS1 !Model for reference fluid viscosity
TC1 !Model for reference fluid thermal conductivity
NUL !Large molecule identifier
1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
0.5493 !Lennard-Jones coefficient sigma [nm] for ECS method !from scaling R134a
370.44 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method !from scaling R134a
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
5.21722e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2
2.92456e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
0.921345 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
0.041091 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
1.08671 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
-0.0216469 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
TK3 !Pointer to critical enhancement auxiliary function
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
TK3 !Simplified thermal conductivity critical enhancement for R-141b of Olchowy and Sengers (1989).
?
?```````````````````````````````````````````````````````````````````````````````
?Olchowy, G.A. and Sengers, J.V.,
? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region,"
? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
9 0 0 0 !# terms: CO2-terms, spare, spare, spare
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
0.63 !Nu (universal exponent)
1.239 !Gamma (universal exponent)
1.03 !R0 (universal amplitude)
0.063 !Z (universal exponent--not used for t.c., only viscosity)
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
0.194e-9 !Xi0 (amplitude) [m]
0.0496 !Gam0 (amplitude) [-]
0.5e-9 !Qd_inverse (modified effective cutoff parameter) [m]; generic number, not fitted to data
719.94 !Tref (reference temperature)=1.5*Tc [K]
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
#STN !---Surface tension---
ST1 !Surface tension model for R-141b of Mulero et al. (2012).
:DOI: 10.1063/1.4768782
?
?```````````````````````````````````````````````````````````````````````````````
?Mulero, A., Cachadiña, I., and Parra, M.I.,
? "Recommended Correlations for the Surface Tension of Common Fluids,"
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
2 !Number of terms in surface tension model
477.5 !Critical temperature used in fit (dummy)
7.3958e-5 0.066331 !Sigma0 and n
0.059941 1.2214
#PS !---Vapor pressure---
PS5 !Vapor pressure equation for R-141b of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 2010.
?
?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc
? are the reducing parameters below, which are followed by rows containing Ni and ti.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
477.5 4212.0 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-7.3784 1.0
5.2955 1.5
-4.6639 1.7
-3.1122 4.2
-1.8972 9.0
#DL !---Saturated liquid density---
DL1 !Saturated liquid density equation for R-141b of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 2010.
?
?Functional Form: D=Dc*[1+SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
? the reducing parameters below, which are followed by rows containing Ni and ti.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
477.5 3.921 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
10.443 0.49
-24.726 0.68
27.718 0.88
-11.220 1.10
0.75848 2.90
#DV !---Saturated vapor density---
DV3 !Saturated vapor density equation for R-141b of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 2010.
?
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
? the reducing parameters below, which are followed by rows containing Ni and ti.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
477.5 3.921 !Reducing parameters
6 0 0 0 0 0 !Number of terms in equation
-3.1177 0.398
-6.8872 1.33
-18.566 3.3
-40.311 6.7
-9.5472 7.0
-124.82 14.0
@END
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