305 lines
13 KiB
Plaintext
305 lines
13 KiB
Plaintext
R1216 !Short name
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116-15-4 !CAS number
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Hexafluoropropene !Full name
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C3F6 !Chemical formula {C3F6}
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Hexafluoropropylene !Synonym
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150.0225192 !Molar mass [g/mol]
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117.654 !Triple point temperature [K]
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242.81 !Normal boiling point [K]
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358.9 !Critical temperature [K]
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3149.528 !Critical pressure [kPa]
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3.8888 !Critical density [mol/L]
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0.333 !Acentric factor
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1.088 !Dipole moment [Debye]; DIPPR DIADEM 2012
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IIR !Default reference state
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10.0 !Version number
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???? !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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1S/C3F6/c4-1(2(5)6)3(7,8)9 !Standard InChI String :InChi:
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HCDGVLDPFQMKDK-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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40377b40 (R1234yf) !Alternative fluid for mixing rules :AltID:
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edc3a7b0 !Hash number from InChI Key :Hash:
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!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
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! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
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! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
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! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
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! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
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! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
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! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
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! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
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! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
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! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
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! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
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! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
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! end of the fluid file is marked with @END. Anything below that is ignored.
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! compiled by E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 11-20-10 YZ, Original version.
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! 12-23-10 MLH, Add predictive transport; experimental data not found.
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! 04-01-13 SH, Add ancillary equations.
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! 04-06-13 EWL, Add dipole moment.
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! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014).
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-1216 of Zhou and Lemmon (2010).
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: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)
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:DOI:
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Equations of State for RE245cb2, RE347mcc, RE245fa2, and R1216
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? to be submitted to J. Phys. Chem. Ref. Data, 2018.
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?
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!```````````````````````````````````````````````````````````````````````````````
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117.654 !Lower temperature limit [K]
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400.0 !Upper temperature limit [K]
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12000.0 !Upper pressure limit [kPa]
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12.89 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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150.0225192 !Molar mass [g/mol]
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117.654 !Triple point temperature [K]
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0.0000936 !Pressure at triple point [kPa]
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12.88 !Density at triple point [mol/L]
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242.81 !Normal boiling point temperature [K]
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0.333 !Acentric factor
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358.9 3149.528 3.8888 !Tc [K], pc [kPa], rhoc [mol/L]
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358.9 3.8888 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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12 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.037582356 1.0 4. 0. !a(i),t(i),d(i),l(i)
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1.4558246 0.3 1. 0.
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-2.701615 1.0 1. 0.
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-0.33573470 1.35 2. 0.
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0.18854950 0.4 3. 0.
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-0.16892060 1.0 3. 2.
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1.122147 1.68 2. 1.
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-0.64050480 2.36 2. 2.
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-0.025931535 0.615 7. 1.
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0.42940852 1.32 1. 1.
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-1.0163408 2.12 1. 2.
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-0.043691328 3.0 1. 3.
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1.2530663 0.82 1. 2. 2. -0.9665 -1.24 1.284 0.67 0. 0. 0.
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-0.54254994 2.85 1. 2. 2. -1.5030 -0.776 0.420 0.925 0. 0. 0.
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-0.15327764 2.83 3. 2. 2. -0.97 -0.86 0.434 0.75 0. 0. 0.
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-0.0092102535 1.67 3. 2. 2. -5.87 -478.0 1.074 0.73 0. 0. 0.
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eta beta gamma epsilon
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EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-1216 of Zhou and Lemmon (2010).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Zhou, Y. and Lemmon, E.W., 2018.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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5.878676 0.0
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9.351559 561.0
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9.192089 1486.0
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7.983222 7595.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-1216 of Zhou and Lemmon (2010).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Zhou, Y. and Lemmon, E.W., 2018.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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4.878676 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-15.4369057809176127 0.0 !aj, ti for [ai*tau**ti] terms
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9.8646536770587776 1.0 !aj, ti for [ai*tau**ti] terms
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9.351559 561.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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9.192089 1486.0
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7.983222 7595.0
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++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
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#TRN !---ECS Transport---
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ECS !Extended Corresponding States model (R134a reference); predictive model; exp. data not found for R-1216.
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:DOI: 10.1021/ie0300880
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Unpublished; uses method described in the following reference:
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
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? a New Correlation for the Viscosity of R134a,"
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? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
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?
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?VISCOSITY
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? Estimated uncertainty 10-20% based on historical performance of model for halogenated refrigerants.
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? Unable to locate experimental data.
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?
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?THERMAL CONDUCTIVITY
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? Unable to locate experimental data.
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? Estimated uncertainty 10-30% based on historical performance of model for halogenated refrigerants.
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?
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?The Lennard-Jones parameters were estimated with the method of Chung.
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?
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!```````````````````````````````````````````````````````````````````````````````
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145.0 !Lower temperature limit [K] viscosity equ. fails below this temp
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400.0 !Upper temperature limit [K]
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12000.0 !Upper pressure limit [kPa]
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12.89 !Maximum density [mol/L]
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FEQ R134A.FLD
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VS1 !Model for reference fluid viscosity
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TC1 !Model for reference fluid thermal conductivity
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NUL !Large molecule identifier
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1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
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0.5144 !Lennard-Jones coefficient sigma [nm] from method Chung
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285.0 !Lennard-Jones coefficient epsilon/kappa [K] from Chung method
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1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
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0.00132 0. 0. 0. !Coefficient, power of T, spare1, spare2
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1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
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1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
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1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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TK3 !Pointer to critical enhancement auxiliary function
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#AUX !---Auxiliary function for the thermal conductivity critical enhancement
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TK3 !Simplified thermal conductivity critical enhancement for R-1216 of Olchowy and Sengers (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Olchowy, G.A. and Sengers, J.V.,
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? "A Simplified Representation For the Thermal Conductivity of Fluids in the Critical Region,"
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? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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9 0 0 0 !# terms: CO2-terms, spare, spare, spare
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1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
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0.63 !Nu (universal exponent)
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1.239 !Gamma (universal exponent)
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1.03 !R0 (universal amplitude)
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0.063 !Z (universal exponent--not used for t.c., only viscosity)
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1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
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0.194e-9 !Xi0 (amplitude) [m]
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0.0496 !Gam0 (amplitude) [-]
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5.835e-10 !Qd_inverse (modified effective cutoff parameter) [m]; R125 value
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538.3 !Tref (reference temperature)=1.5*Tc [K]
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~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
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#STN !---Surface tension---
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ST1 !Surface tension model for R-1216 of Mulero et al. (2014).
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:DOI: 10.1063/1.4878755
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Mulero, A. and Cachadiña, I.,
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? "Recommended Correlations for the Surface Tension of Several Fluids
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? Included in the REFPROP Program,"
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? J. Phys. Chem. Ref. Data, 43, 023104, 2014.
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? doi: 10.1063/1.4878755
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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2 !Number of terms in surface tension model
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358.9 !Critical temperature used in fit (dummy)
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0.053876 1.0944 !Sigma0 and n
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0.038318 2.3239
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#PS !---Vapor pressure---
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PS5 !Vapor pressure equation for R-1216 of Herrig (2013).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Herrig, S., 2013.
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?
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?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc
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? are the reducing parameters below, which are followed by rows containing Ni and ti.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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358.90 3149.528 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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-7.9011 1.0
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3.1506 1.5
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-3.0852 2.0
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-4.2112 4.5
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-15.438 19.0
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#DL !---Saturated liquid density---
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DL1 !Saturated liquid density equation for R-1216 of Herrig (2013).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Herrig, S., 2013.
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?
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?Functional Form: D=Dc*[1+SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
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? the reducing parameters below, which are followed by rows containing Ni and ti.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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358.90 3.8888 !Reducing parameters
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6 0 0 0 0 0 !Number of terms in equation
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1.7159 0.31
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2.3953 0.97
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-5.8035 1.7
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10.749 2.4
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-10.537 3.2
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4.7535 4.1
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#DV !---Saturated vapor density---
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DV3 !Saturated vapor density equation for R-1216 of Herrig (2013).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Herrig, S., 2013.
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?
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?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
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? the reducing parameters below, which are followed by rows containing Ni and ti.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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358.90 3.8888 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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-2.4969 0.353
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-5.8935 1.05
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-16.846 2.74
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-55.082 6.0
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-140.43 13.3
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@END
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