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 Cachadiņa, 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 c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890