R142b !Short name 75-68-3 !CAS number 1-Chloro-1,1-difluoroethane !Full name CClF2CH3 !Chemical formula {C2H3ClF2} HCFC-142b !Synonym 100.49503 !Molar mass [g/mol] 142.72 !Triple point temperature [K] 264.03 !Normal boiling point [K] 410.26 !Critical temperature [K] 4055.0 !Critical pressure [kPa] 4.438 !Critical density [mol/L] 0.2321 !Acentric factor 2.14 !Dipole moment [Debye]; value from REFPROP v5.0 IIR !Default reference state 10.0 !Version number 2517 !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 2310. !GWP (IPCC 2007) :GWP: 0.06 !ODP (WMO 2010) :ODP: 20000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A2 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C2H3ClF2/c1-2(3,4)5/h1H3 !Standard InChI String :InChi: BHNZEZWIUMJCGF-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: f2a8b2e0 !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 ! 05-23-96 MM, Original version. ! 04-12-01 EWL, Add Lemmon and Span short EOS. ! 05-08-02 MLH, Add LJ parameters, k, eta fits. ! 03-13-03 EWL, Replace cp0 equation. ! 01-27-04 EWL, Add final coefficients to EOS. ! 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). ! 01-05-16 MLH, Change TK6 to TK3. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for R-142b of Lemmon and Span (2006). :TRUECRITICALPOINT: 410.26 4.438 !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 in density are 0.3% in the liquid phase below 370 K, 1% ? at higher temperatures in the liquid and supercritical regions, and 0.5% in ? the vapor phase. Uncertainties for other properties are 0.5% for vapor ? pressure, 2% for heat capacities and liquid sound speeds, and 0.2% for ? vapor sound speeds. ? !``````````````````````````````````````````````````````````````````````````````` 142.72 !Lower temperature limit [K] 470.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 14.44 !Maximum density [mol/L] CPP !Pointer to Cp0 model 100.49503 !Molar mass [g/mol] 142.72 !Triple point temperature [K] 0.003632 !Pressure at triple point [kPa] 14.44 !Density at triple point [mol/L] 264.03 !Normal boiling point temperature [K] 0.2321 !Acentric factor 410.26 4055.0 4.438 !Tc [K], pc [kPa], rhoc [mol/L] 410.26 4.438 !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 1.0038 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.7662 1.25 1. 0. 0.42921 1.5 1. 0. 0.081363 0.25 3. 0. 0.00024174 0.875 7. 0. 0.48246 2.375 1. 1. 0.75542 2.0 2. 1. -0.007430 2.125 5. 1. -0.41460 3.5 1. 2. -0.016558 6.5 1. 2. -0.10644 4.75 4. 2. -0.021704 12.5 2. 3. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-142b 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 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0 0.0 5.0385 473.0 6.8356 1256.0 4.0591 2497.0 2.8136 6840.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-142b of Lemmon and Span (2006). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W. and Span, R., 2006. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 4 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 -12.6016704500950851 0.0 !aj, ti for [ai*tau**ti] terms 8.316026972375175 1.0 !aj, ti for [ai*tau**ti] terms 5.0385 473.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 6.8356 1256.0 4.0591 2497.0 2.8136 6840.0 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for R-142b. ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W. and Span, R., 2006. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 4 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 -12.6016527149 0.0 !aj, ti for [ai*tau**ti] terms 8.3160183265 1.0 5.0385 -1.1529274119 !aj, ti for [ai*log(1-exp(ti*tau)] terms 6.8356 -3.0614732121 4.0591 -6.0863842441 2.8136 -16.6723541169 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); fitted to data for R-142b. :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.A., Laesecke, A., and Nieto de Castro, C.A., "Polarized Transient Hot Wire Thermal Conductivity Measurements," Fluid Phase Equilib., 80:275-286, 1992. doi: 10.1016/0378-3812(92)87074-W ? Sousa, A.T., Fialho, P.S., Nieto de Castro, C.A., Tufeu, R., and LeNeindre, B., "The Thermal Conductivity of 1-Chloro-1,1-Difluoroethane," Int. J. Thermophys., 13(3):383, 1992. doi: 10.1007/BF00503878 ? Tanaka, Y., Nakata, M., and Makita, T., "Thermal Conductivity of Gaseous HFC-134a, HFC-143a, HCFC-141b, and HCFC-142b," Int. J. Thermophys., 12:949-963, 1991. ? Yata, J., Hori, M., Kurahashi, T., and Minamiyama, T., "Thermal Conductivity of Alternative Fluorocarbons in Liquid Phase," Fluid Phase Equilib., 80:287-296, 1992. ? Kim, S.H., Kim, D.S., Kim, M.S., and Ro, S.T., "The Thermal Conductivity of R22, R142b, R152a, and Their Mixtures in the Liquid State," Int. J. Thermophys., 14:937-50, 1993. doi: 10.1007/BF00502116 ? Average absolute deviations of the fit from the experimental data are: ? Perkins: 0.93%; Sousa: 2.53%; Tanaka: 2.77%; Yata: 1.72%; Kim: 0.76%. ? Overall: 1.99%. ? ?VISCOSITY ? The ECS parameters for viscosity were based in part on the data of: ? Kumagai, A. and Yokoyama, C., "Revised Viscosities of Saturated Liquid Halocarbon Refrigerants from 273 to 353 K," Int. J. Thermophys., 21(4):909-912, 2000. ? Arnemann, M. and Kruse, H., "Liquid Viscosities of the Non-Azeotropic Binary Refrigerant Mixtures R22/R114, R22/R152a, R22/R142b," Actes Congr. Int. Froid, 18(2):379-383, 1991. ? Average absolute deviations of the fit from the experimental data are: ? Kumagai: 2.26%; Arnemann: 2.27%. ? Overall: 2.26%. ? ?The Lennard-Jones parameters were taken from Nabizadeh, H. and Mayinger, F., "Viscosity of Gaseous R123, R134a and R142b," High Temp.-High Press., 24:221, 1992. ? !``````````````````````````````````````````````````````````````````````````````` 142.72 !Lower temperature limit [K] 470.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 14.44 !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) 0.5362 !Lennard-Jones coefficient sigma [nm] for ECS method 278.20 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.000940725 0. 0. 0. !Coefficient, power of T, spare1, spare2 0.988196e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 0.971602 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 0.019181 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 1.07494 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0177916 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-142b 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) [-] 0.615654e-9 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data 615.39 !Tref (reference temperature)=1.5*Tc [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-142b 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 410.26 !Critical temperature used in fit (dummy) 0.05685 1.237 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-142b 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. ! 410.26 4055.0 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.3074 1.0 2.3186 1.5 -2.3278 2.2 -3.2761 4.8 0.42103 6.2 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-142b 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. ! 410.26 4.438 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 17.162 0.53 -47.495 0.71 57.171 0.9 -25.404 1.1 1.5855 2.3 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-142b 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. ! 410.26 4.438 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -3.1460 0.408 -6.5221 1.28 -18.006 3.2 -46.694 6.6 -2.6087 7.0 -110.20 14.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890