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一些优化：CAN和PLC地址的优化

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R1216 !Short name
116-15-4 !CAS number
Hexafluoropropene !Full name
C3F6 !Chemical formula {C3F6}
Hexafluoropropylene !Synonym
150.0225192 !Molar mass [g/mol]
117.654 !Triple point temperature [K]
242.81 !Normal boiling point [K]
358.9 !Critical temperature [K]
3149.528 !Critical pressure [kPa]
3.8888 !Critical density [mol/L]
0.333 !Acentric factor
1.088 !Dipole moment [Debye]; DIPPR DIADEM 2012
IIR !Default reference state
10.0 !Version number
???? !UN Number :UN:
halocb !Family :Family:
???? !Heating value (upper) [kJ/mol] :Heat:
1S/C3F6/c4-1(2(5)6)3(7,8)9 !Standard InChI String :InChi:
HCDGVLDPFQMKDK-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
40377b40 (R1234yf) !Alternative fluid for mixing rules :AltID:
edc3a7b0 !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
! 11-20-10 YZ, Original version.
! 12-23-10 MLH, Add predictive transport; experimental data not found.
! 04-01-13 SH, Add ancillary equations.
! 04-06-13 EWL, Add dipole moment.
! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014).
________________________________________________________________________________
#EOS !---Equation of state---
FEQ !Helmholtz equation of state for R-1216 of Zhou and Lemmon (2010).
:TRUECRITICALPOINT: 358.9 3.8888 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
:DOI:
?
?```````````````````````````````````````````````````````````````````````````````
?Equations of State for RE245cb2, RE347mcc, RE245fa2, and R1216
? to be submitted to J. Phys. Chem. Ref. Data, 2018.
?
!```````````````````````````````````````````````````````````````````````````````
117.654 !Lower temperature limit [K]
400.0 !Upper temperature limit [K]
12000.0 !Upper pressure limit [kPa]
12.89 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
150.0225192 !Molar mass [g/mol]
117.654 !Triple point temperature [K]
0.0000936 !Pressure at triple point [kPa]
12.88 !Density at triple point [mol/L]
242.81 !Normal boiling point temperature [K]
0.333 !Acentric factor
358.9 3149.528 3.8888 !Tc [K], pc [kPa], rhoc [mol/L]
358.9 3.8888 !Reducing parameters [K, mol/L]
8.314472 !Gas constant [J/mol-K]
12 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.037582356 1.0 4. 0. !a(i),t(i),d(i),l(i)
1.4558246 0.3 1. 0.
-2.701615 1.0 1. 0.
-0.33573470 1.35 2. 0.
0.18854950 0.4 3. 0.
-0.16892060 1.0 3. 2.
1.122147 1.68 2. 1.
-0.64050480 2.36 2. 2.
-0.025931535 0.615 7. 1.
0.42940852 1.32 1. 1.
-1.0163408 2.12 1. 2.
-0.043691328 3.0 1. 3.
1.2530663 0.82 1. 2. 2. -0.9665 -1.24 1.284 0.67 0. 0. 0.
-0.54254994 2.85 1. 2. 2. -1.5030 -0.776 0.420 0.925 0. 0. 0.
-0.15327764 2.83 3. 2. 2. -0.97 -0.86 0.434 0.75 0. 0. 0.
-0.0092102535 1.67 3. 2. 2. -5.87 -478.0 1.074 0.73 0. 0. 0.
eta beta gamma epsilon
EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
#AUX !---Auxiliary function for Cp0
CPP !Ideal gas heat capacity function for R-1216 of Zhou and Lemmon (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Zhou, Y. and Lemmon, E.W., 2018.
?
!```````````````````````````````````````````````````````````````````````````````
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
5.878676 0.0
9.351559 561.0
9.192089 1486.0
7.983222 7595.0
#AUX !---Auxiliary function for PX0
PX0 !Helmholtz energy ideal-gas function for R-1216 of Zhou and Lemmon (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Zhou, Y. and Lemmon, E.W., 2018.
?
!```````````````````````````````````````````````````````````````````````````````
1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
4.878676 1.0 !ai, ti for [ai*log(tau**ti)] terms
-15.4369057809176127 0.0 !aj, ti for [ai*tau**ti] terms
9.8646536770587776 1.0 !aj, ti for [ai*tau**ti] terms
9.351559 561.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
9.192089 1486.0
7.983222 7595.0
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
#TRN !---ECS Transport---
ECS !Extended Corresponding States model (R134a reference); predictive model; exp. data not found for R-1216.
: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
?
?VISCOSITY
? Estimated uncertainty 10-20% based on historical performance of model for halogenated refrigerants.
? Unable to locate experimental data.
?
?THERMAL CONDUCTIVITY
? Unable to locate experimental data.
? Estimated uncertainty 10-30% based on historical performance of model for halogenated refrigerants.
?
?The Lennard-Jones parameters were estimated with the method of Chung.
?
!```````````````````````````````````````````````````````````````````````````````
145.0 !Lower temperature limit [K] viscosity equ. fails below this temp
400.0 !Upper temperature limit [K]
12000.0 !Upper pressure limit [kPa]
12.89 !Maximum density [mol/L]
FEQ R134A.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)
0.5144 !Lennard-Jones coefficient sigma [nm] from method Chung
285.0 !Lennard-Jones coefficient epsilon/kappa [K] from Chung method
1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
0.00132 0. 0. 0. !Coefficient, power of T, spare1, spare2
1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
1.0 0. 0. 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-1216 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) [-]
5.835e-10 !Qd_inverse (modified effective cutoff parameter) [m]; R125 value
538.3 !Tref (reference temperature)=1.5*Tc [K]
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
#STN !---Surface tension---
ST1 !Surface tension model for R-1216 of Mulero et al. (2014).
:DOI: 10.1063/1.4878755
?
?```````````````````````````````````````````````````````````````````````````````
?Mulero, A. and Cachadiña, I.,
? "Recommended Correlations for the Surface Tension of Several Fluids
? Included in the REFPROP Program,"
? J. Phys. Chem. Ref. Data, 43, 023104, 2014.
? doi: 10.1063/1.4878755
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
2 !Number of terms in surface tension model
358.9 !Critical temperature used in fit (dummy)
0.053876 1.0944 !Sigma0 and n
0.038318 2.3239
#PS !---Vapor pressure---
PS5 !Vapor pressure equation for R-1216 of Herrig (2013).
?
?```````````````````````````````````````````````````````````````````````````````
?Herrig, S., 2013.
?
?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. !
358.90 3149.528 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-7.9011 1.0
3.1506 1.5
-3.0852 2.0
-4.2112 4.5
-15.438 19.0
#DL !---Saturated liquid density---
DL1 !Saturated liquid density equation for R-1216 of Herrig (2013).
?
?```````````````````````````````````````````````````````````````````````````````
?Herrig, S., 2013.
?
?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. !
358.90 3.8888 !Reducing parameters
6 0 0 0 0 0 !Number of terms in equation
1.7159 0.31
2.3953 0.97
-5.8035 1.7
10.749 2.4
-10.537 3.2
4.7535 4.1
#DV !---Saturated vapor density---
DV3 !Saturated vapor density equation for R-1216 of Herrig (2013).
?
?```````````````````````````````````````````````````````````````````````````````
?Herrig, S., 2013.
?
?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. !
358.90 3.8888 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-2.4969 0.353
-5.8935 1.05
-16.846 2.74
-55.082 6.0
-140.43 13.3
@END
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