R124 !Short name 2837-89-0 !CAS number 1-Chloro-1,2,2,2-tetrafluoroethane !Full name CHClFCF3 !Chemical formula {C2HClF4} HCFC-124 !Synonym 136.4762 !Molar mass [g/mol] 74. !Triple point temperature [K] 261.187 !Normal boiling point [K] 395.425 !Critical temperature [K] 3624.295 !Critical pressure [kPa] 4.1033156 !Critical density [mol/L] (560 kg/m^3) 0.28810 !Acentric factor 1.469 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Phys. Chem. 95:3860-3866. IIR !Default reference state 10.0 !Version number 1021 !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 609. !GWP (IPCC 2007) :GWP: 0.02 !ODP (WMO 2010) :ODP: 10000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C2HClF4/c3-1(4)2(5,6)7/h1H !Standard InChI String :InChi: BOUGCJDAQLKBQH-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 36953260 !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 M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado ! 12-31-96 MM, Original version. ! 05-22-02 MLH, Refit transport, changed ref.fluid to propane. ! 04-19-04 MLH, Update transport references. ! 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-124 of de Vries et al. (1995). :TRUECRITICALPOINT: 395.425 4.098136 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?de Vries, B., Tillner-Roth, R., and Baehr, H.D., ? "Thermodynamic Properties of HCFC 124," ? 19th International Congress of Refrigeration, The Hague, The Netherlands, ? International Institute of Refrigeration, IVa:582-589, 1995. ? ?The uncertainties of the equation of state are 0.05% in density, 1% in heat ? capacity, and 1% in the speed of sound, except in the critical region. ? The uncertainty in vapor pressure is 0.1%. ? !``````````````````````````````````````````````````````````````````````````````` 120.0 !Lower temperature limit [K] 470.0 !Upper temperature limit [K] 40000.0 !Upper pressure limit [kPa] 13.6 !Maximum density [mol/L] CPP !Pointer to Cp0 model 136.475 !Molar mass [g/mol] 74. !Triple point temperature [K] 0.00000000000003228 !Pressure at triple point [kPa] 14.5 !Density at triple point [mol/L] 261.187 !Normal boiling point temperature [K] 0.28810 !Acentric factor 395.425 3624.295 4.1033156 !Tc [K], pc [kPa], rhoc [mol/L] 395.425 4.1033156 !Reducing parameters [K, mol/L] 8.314471 !Gas constant [J/mol-K] 20 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -0.01262962 2.0 1. 0. !a(i),t(i),d(i),l(i) 2.168373 0.5 1. 0. -3.330033 1.0 1. 0. 0.1610361 0.5 2. 0. -0.9666145e-4 2.5 2. 0. 0.0119131 -1.0 3. 0. -0.002880217 1.0 5. 0. 0.001681346 0.0 6. 0. 0.1594968e-4 -0.5 8. 0. 0.1289674 1.5 2. 1. 0.1182213e-4 1.0 12. 1. -0.4713997 2.5 1. 2. -0.2412873 -0.25 1. 2. 0.6868066 1.0 1. 2. -0.08621095 5.0 1. 2. 0.4728645e-5 2.0 15. 2. 0.01487933 15.0 3. 3. -0.03001338 20.0 3. 3. 0.001849606 15.0 4. 4. 0.0004126073 45.0 9. 4. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-124 of de Vries et al. (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?de Vries, B., Tillner-Roth, R., and Baehr, H.D., ? ?Note: de Vries et al. give a Helmholtz form for the ideal gas term; it ? has been converted to a Cp0 form, by the transform: ? ?Cp0/R = (1 + a_3) - 2a_4*Tr - 6a_5*Tr^2 - 12a_6*Tr^3 ? where T_r = T/Tcrit, ? and the a_i are the original coefficients given by de Vries. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 395.425 8.314471 !Reducing parameters for T, Cp0 4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.175638 0.0 ! = 1 + a_3 (the a_i are coeff of de Vries) 14.77947 1.0 ! = -2a_4 -5.2420986 2.0 ! = -6a_5 1.3381596 3.0 ! = -12a_6 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-124 of de Vries et al. (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?de Vries, B., Tillner-Roth, R., and Baehr, H.D., ? ?Note: de Vries et al. give a Helmholtz form for the ideal gas term; it ? has been converted to a Cp0 form, by the transform: ? ?Cp0/R = (1 + a_3) - 2a_4*Tr - 6a_5*Tr^2 - 12a_6*Tr^3 ? where T_r = T/Tcrit, ? and the a_i are the original coefficients given by de Vries. ? !``````````````````````````````````````````````````````````````````````````````` 1 5 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 2.175638 1.0 !ai, ti for [ai*log(tau**ti)] terms -11.6694278205254687 0.0 !aj, ti for [ai*tau**ti] terms 9.8760554938431273 1.0 !aj, ti for [ai*tau**ti] terms 0.0373761648858823 -1.0 -0.335256293183e-04 -2.0 0.216429045539e-07 -3.0 -------------------------------------------------------------------------------- @EOS !---Equation of state--- BWR !MBWR equation of state for R-124 of Younglove and McLinden (1994). ? ?``````````````````````````````````````````````````````````````````````````````` ?McLinden, M.O., Younglove, B.A., and Sandarusi, J., ? "Measurement of the PVT properties and formulation of an equation of state ? for refrigerant 124 (1-chloro-1,2,2,2-tetrafluoroethane)," 1994. ? (unpublished manuscript). ? !``````````````````````````````````````````````````````````````````````````````` 120.0 !Lower temperature limit [K] 475.0 !Upper temperature limit [K] 36000.0 !Upper pressure limit [kPa] 13.98 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 136.4762 !Molar mass [g/mol] 74.0 !Triple point temperature [K] 0.00000000032 !Pressure at triple point [kPa] 14.54 !Density at triple point [mol/L] 261.212 !Normal boiling point temperature [K] 0.28783 !Acentric factor 395.62 3637.0 4.101527 !Tc [K], pc [kPa], rhoc [mol/L] 395.62 4.101527 !Reducing parameters [K, mol/L] 4.101527 !gamma 0.08314471 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term -0.0195111839846 2.99978502039 -84.5849168162 14672.0754658 -2325493.36572 0.000938866046628 -4.25069993257 3048.591316 2213148.2991 -0.601971995213e-4 1.00335188373 -468.461812962 -0.00927654315163 -12.5426962519 -2285.34445089 1.68197835599 -0.0537322295315 15.7915168095 -0.550297175283 -2443499.54189 -62515301.6263 -156149.23182 0.344268154495e+10 -2892.12955106 108351.996828 -40.4809912845 -2205872.92481 -0.564677367857 175.581172016 -0.000762146322899 -2.10617958917 31.9236066221 @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for R-124. ? ?``````````````````````````````````````````````````````````````````````````````` ?McLinden, M.O., Younglove, B.A., and Sandarusi, J., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 395.62 8.314471 !Reducing parameters for T, Cp0 4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.20532538 0.0 13.4403357 1.0 -2.32192933 2.0 -0.422826803 3.0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); fitted to data for R-124. :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: ? Yata, J., Minamiyana, T., and Tanaka, S., "Measurement of Thermal Conductivity of Liquid Fluorocarbons," Int. J. Thermophys., 5(2):209-218, 1984. ? Yata, J., Hori, M., Kurahashi, T., and Minamiyama, T., "Thermal Conductivity of Alternative Fluorocarbons in Liquid Phase," Fluid Phase Equilib., 80:287-296, 1992. doi: 10.1016/0378-3812(92)87075-X ? 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. ? Assael, M.J., Malamataris, N., and Karagiannidis, L., "Measurements of the Thermal Conductivity of Refrigerants in the Vapor Phase," Int. J. Thermophys., 18(2):341-352, 1997. doi: 10.1007/BF02575165 ? Fellows, B.R., Richard, R.G., and Shankland, I.R., "Thermal Conductivity Data for Some Environmentally Acceptable Fluorocarbons," Thermal Conductivity 21, Plenum Press, NY, 1990. ? Perkins, R.A., personal communication, NIST, 2001. perkins@boulder.nist.gov ? Average absolute deviations of the fit from the experimental data are: ? Yata, 1992: 0.68%; Assael, 1995: 0.66%; Yata, 1984: 1.39%; Assael, 1997: 0.90%; ? Fellows, 1990: 3.03%; Perkins, 2001: 2.61%. ? Overall: 2.45%. ? ?VISCOSITY ? The ECS parameters for viscosity were based in part on the data of: ? Assael, M.J., Polimatidou, S.K., "Measurements of the Viscosity of Liquid R22, R124, and R125 in the Temperature Range 273-333 K," Int. J. Thermophys., 15(5):779-790, 1994. doi: 10.1007/BF01447094 ? Assael, M.J., Polimatidou, S.K., "Measurements of the Viscosity of Refrigerants in the Vapor Phase," Int. J. Thermophys., 18(2):353-366, 1997. doi: 10.1007/BF02575166 ? Diller, D.E. and Peterson, S.M., "Measurements of the Viscosities of Saturated and Compressed Fluid 1-Chloro-1,2,2,2-Tetrafluoroethane (R124) and Pentafluoroethane (R125) at Temperatures between 120 and 420 K," Int. J. Thermophys., 14(1):55-66, 1993. doi: 10.1007/BF00522661 ? Ripple, D. and Matar, O., "Viscosity of the Saturated Liquid Phase of Six Halogenated Compounds and Three Mixtures," J. Chem. Eng. Data, 38:560-564, 1993. doi: 10.1021/je00012a021 ? Average absolute deviations of the fit from the experimental data are: ? Assael, 1994: 0.92%; Assael, 1997: 0.80%; Diller: 4.99%; Ripple: 1.20%. ? Overall: 3.56%. ? ?The Lennard-Jones parameters were taken from Dowdell, D.C. and Matthews, G.P., "Gas Viscosities and Intermolecular Interactions of Replacement Refrigerants HCFC 123 (2,2-Dichloro- 1,1,1-Trifluoroethane), HCFC 124 (2-Chloro-1,1,1,2-Tetrafluoroethane), and HFC 134a (1,1,1,2-Tetrafluoroethane)," J. Chem. Soc. Faraday Trans., 89:3545-3552, 1993. doi: 10.1039/ft9938903545 ? !``````````````````````````````````````````````````````````````````````````````` 120.0 !Lower temperature limit [K] 470.0 !Upper temperature limit [K] 40000.0 !Upper pressure limit [kPa] 13.6 !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) 0.5501 !Lennard-Jones coefficient sigma [nm] for ECS method 275.8 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.0011769 0. 0. 0. !Coefficient, power of T, spare1, spare2 0.678397e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.04253 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 0.00138528 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 1.08978 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0154229 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-124 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.e-10 !Qd_inverse (modified effective cutoff parameter) [m]; not fitted to data 593.1375 !Tref (reference temperature)=1.5*Tc [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-124 of Mulero et al. (2012). :DOI: 10.1063/1.4768782 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A., Cachadiņa, 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. ! 1 !Number of terms in surface tension model 395.425 !Critical temperature used in fit (dummy) 0.05175 1.197 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-124 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. ! 395.425 3624.295 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.5146 1.0 3.7481 1.5 -3.0124 1.68 -3.7808 3.8 -0.53114 8.0 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-124 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. ! 395.425 4.1033156 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 1.9127 0.345 0.67778 0.74 -0.035129 1.2 0.30407 2.6 0.069503 7.2 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-124 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. ! 395.425 4.1033156 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -2.8551 0.388 -6.3850 1.17 -17.616 3.0 -37.828 6.0 -23.785 8.0 -134.59 15.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890