R123 !short name (same as file name) 306-83-2 !CAS number 2,2-dichloro-1,1,1-trifluoroethane HCFC-123 !synonym1 R-123 !synonym2 152.931 !molecular weight [g/mol] 166.00 !triple pt temperature [K] 300.973 !normal boiling pt [K] 456.831 !critical temperature [K] 3661.8 !critical pressure [kPa] 3.596417 !critical density [mol/L] 0.28192 !acentric factor 1.356 !dipole moment [Debye]; Meyer & Morrison JCED 36:409 (1991) IIR !default reference state 6.001 !version number ! compiled by M. McLinden, NIST Thermophysics Division, Boulder, Colorado ! 10-10-95 MM, original version ! 03-15-96 MM, add transport correlations compiled by S.A. Klein ! 03-18-96 MM, add dipole moment ! 06-17-96 MM, add thermal conductivity coefficients fitted by S.A. Klein ! 08-19-96 MM, add surface tension fit ! 01-31-97 MM, change pointer for ECS reference viscosity from VS3 to VS1 ! put viscosity model of Tanaka and Sotani into new VS1 form ! 02-20-97 MM, add default reference state ! 02-25-97 MM, add thermal conductivity correlation of Laesecke ! 02-26-97 MM, add version number and pointer to visc critical enhancement (both future use) ! 03-11-97 MM, modify ECS-transport to new format ! 03-25-97 MM, set Psi,Chi coeff in ECS-transport to 1,0 pending refit of data ! 08-21-97 MM, purge exponentials from values read by GUI (e.g. model limits) ! 10-24-97 MM, read in f_int term in Eucken correlation in ECS method for t.c. ! change reference fluid EOS for ECS-transport from BWR to FEQ #EOS !equation of state specification BWR MBWR equation of state; Younglove & McLinden (1994). ?LITERATURE REFERENCE \ ?B.A. Younglove and M.O. McLinden. An international standard equation-of-state ? formulation of the thermodynamic properties of refrigerant 123 ? (2,2-dichloro-1,1,1-trifluoroethane). ? J. Phys. Chem. Ref. Data 23:731-779 (1994). \ ?\ ?ABSTRACT \ ?A modified Bennedict-Webb-Rubin (MBWR) equation of state has been developed ? for Refrigerant 123 (2,2-dichloro-1,1,1-trifluoroethane) based on recently ? measured thermodynamic property data and data available from the literature. ? Single-phase pressure-volume-temperature (PVT), heat capacity, and sound speed ? data, as well as second virial, vapor pressure, and saturated liquid and ? saturated vapor density data, were used with multiproperty linear least ? squares fitting techniques to fit the 32 adjustable coefficients of the MBWR ? equation. Coefficients fro the equation of state and for ancillary equations ? representing the vapor pressure, saturated liquid and saturated vapor ? densities, and ideal gas heat capacity are given. While the measurements ? cover differing ranges of temperature and pressure, the MBWR formulation is ? applicable along the saturation line and in the liquid, vapor, and ? supercritical regions at temperatures from 166 to 500 K with pressures to ? 40 MPa and densities to 11.6 mol/L (1774 kg/m3). This formulation has been ? selected as an international standard based on an evaluation of the available ? equations of state by a group working under the auspices of the International ? Energy Agency. ? !end of info section 166.0 !lower temperature limit [K] 600.0 !upper temperature limit [K] 40000.0 !upper pressure limit [kPa] 11.60 !maximum density [mol/L] CPP !pointer to Cp0 model 152.931d0 !molecular weight [g/mol] 166.00d0 !triple point temperature [K] 0.00004d0 !pressure at triple point [kPa] 11.60d0 !density at triple point [mol/L] 300.973d0 !normal boiling point temp [K] 0.28192d0 !acentric factor 456.831d0 3661.8d0 3.596417d0 !Tc [K], pc [kPa], rhoc [mol/L] 456.831d0 3.596417d0 !reducing parameters [K, mol/L] 3.596417d0 !gamma 0.08314510d0 !gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term -0.657453133659d-02 0.293479845842d+01 -0.989140469845d+02 0.201029776013d+05 -0.383566527886d+07 0.227587641969d-02 -0.908726819450d+01 0.434181417995d+04 0.354116464954d+07 -0.635394849670d-03 0.320786715274d+01 -0.131276484299d+04 -0.116360713718d+00 -0.113354409016d+02 -0.537543457327d+04 0.258112416120d+01 -0.106148632128d+00 0.500026133667d+02 -0.204326706346d+01 -0.249438345685d+07 -0.463962781113d+09 -0.284903429588d+06 0.974392239902d+10 -0.637314379308d+04 0.314121189813d+06 -0.145747968225d+03 -0.843830261449d+07 -0.241138441593d+01 0.108508031257d+04 -0.106653193965d-01 -0.121343571084d+02 -0.257510383240d+03 @EOS !equation of state specification FEQ Helmholtz transform of MBWR EOS of Younglove & McLinden (1994) ?LITERATURE REFERENCE \ ?B.A. Younglove and M.O. McLinden. An international standard equation-of-state ? formulation of the thermodynamic properties of refrigerant 123 ? (2,2-dichloro-1,1,1-trifluoroethane). ? J. Phys. Chem. Ref. Data 23:731-779 (1994). \ ?\ ?transformed into the fundamental (Helmholtz) form by E.W. Lemmon, ? University of Idaho, 1996. ? !end info 166.0 !lower temperature limit [K] 600.0 !upper temperature limit [K] 40000.0 !upper pressure limit [kPa] 11.60 !maximum density [mol/L] CPP !pointer to Cp0 model 152.931d0 !molecular weight [g/mol] 166.00d0 !triple point temperature [K] 0.00004d0 !pressure at triple point [kPa] 11.60d0 !density at triple point [mol/L] 300.973d0 !normal boiling point temp [K] 0.28192d0 !acentric factor 456.831d0 3661.8d0 3.596417d0 !Tc [K], pc [kPa], rhoc [mol/L] 456.831d0 3.596417d0 !reducing parameters [K, mol/L] 8.314510d0 !gas constant [J/mol-K] 40 4 !Nterm, Ncoeff per term -0.100242647494E+02 3.000 0.00 0 !a(i),t(i),d(i),l(i) -0.280607656419E+00 4.000 0.00 0 0.206814471606E-01 5.000 0.00 0 -0.284379431451E+00 0.000 1.00 0 0.593928110321E+01 0.500 1.00 0 -0.936560389528E+01 1.000 1.00 0 0.416660793675E+01 2.000 1.00 0 -0.174023292951E+01 3.000 1.00 0 0.177019905365E+00 0.000 2.00 0 -0.154721692260E+01 1.000 2.00 0 0.161820495590E+01 2.000 2.00 0 0.288903529383E+01 3.000 2.00 0 -0.118493874757E+00 0.000 3.00 0 0.130952266209E+01 1.000 3.00 0 -0.117308103711E+01 2.000 3.00 0 -0.128125131950E+00 1.000 4.00 0 -0.786087387513E-01 2.000 5.00 0 -0.816000499305E-01 3.000 5.00 0 0.536451054311E-01 2.000 6.00 0 -0.680078211929E-02 2.000 7.00 0 0.701264082191E-02 3.000 7.00 0 -0.901762397311E-03 3.000 8.00 0 0.100242647494E+02 3.000 0.00 2 0.280607656419E+00 4.000 0.00 2 -0.206814471606E-01 5.000 0.00 2 0.798923878145E+01 3.000 2.00 2 -0.547972072476E+00 4.000 2.00 2 -0.206814470584E-01 5.000 2.00 2 0.249142724365E+01 3.000 4.00 2 -0.273986034884E+00 4.000 4.00 2 0.236001863614E+00 5.000 4.00 2 0.540528251211E+00 3.000 6.00 2 -0.600457561959E-01 4.000 6.00 2 0.786672874826E-01 5.000 6.00 2 0.708085874508E-01 3.000 8.00 2 -0.150114389748E-01 4.000 8.00 2 0.182205199477E-02 5.000 8.00 2 0.314978575163E-02 3.000 10.00 2 0.784455573794E-02 4.000 10.00 2 0.364410397155E-03 5.000 10.00 2 #AUX !auxiliary model specification CPP polynomial fit for ideal gas heat capacity; Younglove & McLinden (1994). ?LITERATURE REFERENCE \ ?B.A. Younglove and M.O. McLinden. An international standard equation-of-state ? formulation of the thermodynamic properties of refrigerant 123 ? (2,2-dichloro-1,1,1-trifluoroethane). ? J. Phys. Chem. Ref. Data 23:731-779 (1994). \ ?\ !end of info section 150.0 !lower temperature limit [K] 500.0 !upper temperature limit [K] 0.00 !upper pressure limit [kPa] 0.00 !maximum density [mol/L] 1.000 1.000 !reducing parameters for T, Cp0 4 0 !Nterms: polynonial, exponential 17.01154d0 0.00 !c(i), power of T 0.4046308d0 1.00 -4.644803d-4 2.00 2.347418d-7 3.00 @TRN !transport model specification ECS Extended Corresponding States model for transport props (R134a ref. fluid). ?LITERATURE REFERENCES \ ?Klein, S.A., McLinden, M.O. and Laesecke, A. (1997). An improved extended ? corresponding states method for estimation of viscosity of pure refrigerants ? and mixtures. Int. J. Refrigeration 20: 208-217.\ ?\ ?Huber, M.L., Friend, D.G. and Ely, J.F. Prediction of the thermal ? conductivity of refrigerants and refrigerant mixtures. ? Fluid Phase Equilibria 80: 249-261 (1992). \ ?\ ?Thermal conductivity data used in the development of the extended corresponding ? states method were taken from:\ ?A Assael, M. J. and A Karagiannidis, E. ? Measurements of the Thermal Conductivity of R22, R123, and R134a in the ? Temperature Range 250-340 K at Pressures up to 30 MPa ? J Int. J. Thermophysics, V 14, N 2. P 183-197, 1993\ ?\ ?Lennard-Jones parameters from:\ ?Nabizadeh, H. and Mayinger, F. Viscosity of gaseous R123, R134a and R142b. ? High Temperatures - High Pressures 24:221 (1992). ?\ !end of info section 166.0 !lower temperature limit [K] 600.0 !upper temperature limit [K] 40000.0 !upper pressure limit [kPa] 11.60 !maximum density [mol/L] FEQ R134a.fld VS1 !model for reference fluid viscosity TC1 !model for reference fluid thermal conductivity 1 !Lennard-Jones flag (0 or 1) (0 => use estimates) 0.5909 !Lennard-Jones coefficient sigma [nm] 275.16 !L-J coefficient epsilon/kB [K] 1 0 0 !number of terms in f_int term in Eucken correlation, spare1, spare 2 1.3200d-3 0.0 0.0 0.0 !coeff, power of T, spare 1, spare 2 0 0 0 !number of terms in psi (visc shape factor): poly,spare1,spare2 0 0 0 !number of terms in chi (t.c. shape factor): poly,spare1,spare2 #ETA !viscosity model specification VS1 pure fluid viscosity model of Tanaka and Sotani (1995). ?LITERATURE REFERENCE \ ?Tanaka, Y. and Sotani, T. Transport Properties (Thermal Conductivity and ? Viscosity). in McLinden, M.O., editor. R123--Thermodynamic and physical ? properties. Paris: International Institute of Refrigeration (1995). \ ? !end of info section 240.0 !lower temperature limit [K] 440.0 !upper temperature limit [K] 20000.0 !upper pressure limit [kPa] 15.90 !maximum density [mol/L] 4 !number of terms associated with dilute-gas function NUL !pointer to collision integral model (not used here) 0.5909 !Lennard-Jones coefficient sigma [nm] 275.16 !Lennard-Jones coefficient epsilon/kB [K] 1.0d0 1.0d0 !reducing parameters for T, eta 0.0d0 0.5d0 !Chapman-Enskog term (not used here) -2.273638d+0 0.0d0 !polynomial term: coeff, power of T 5.099859d-2 1.0d0 -2.402786d-5 2.0d0 0 !# initial density terms (these are merged with residual term) 1 6 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; demoninator of rat. poly; numer of exponential; demon exponential 1.0d0 6.538897d-3 1.0d0 !reducing parameters for T, rho (= 1/MW), eta 1.828263d+3 0.00 0.00 0.00 0 !rho_0; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present] -1.762849d+2 0.00 0.00 0.00 0 !d0/rho_0 -2.226484d-2 0.00 1.00 0.00 0 !const term in Eqn 2.8 (the initial density term) 5.550623d-5 1.00 1.00 0.00 0 !temperature term in Eqn 2.8 -1.009812d-1 0.00 1.00 0.00 0 !d1 in Eqn 2.9 6.161902d-5 0.00 2.00 0.00 0 !d2 -8.840480d-8 0.00 3.00 0.00 0 !d3 -3.222951d+5 0.00 0.00 0.00 0 !d0 in numerator of rational polynomial 1.000000d+0 0.00 1.00 0.00 0 !rho in denominator of rational polynomial -1.000000d+0 0.00 0.00 1.00 0 !rho_0 in denominator of rational polynomial NUL !pointer to critical enhancement auxiliary function (none used) #TCX !thermal conductivity model specification TC1 pure fluid thermal conductivity model of Laesecke et al. (1996) ?LITERATURE REFERENCE\ ?Laesecke, A., Perkins, R.A. and Howley, J.B. (1996). An improved correlation ? for the thermal conductivity of HCFC123 (2,2-dichloro-1,1,1-trifluoroethane). ? Int. J. Refrigeration 19: 231-238.\ ?\ !end of info section 180.0 !lower temperature limit [K] 480.0 !upper temperature limit [K] 67000.0 !upper pressure limit [kPa] 12.42 !maximum density [mol/L] (= 1900 kg/m^3) 2 0 !# terms for dilute gas function: numerator, denominator 1.0d0 1.0d0 !reducing parameters for T, tcx -0.00778d0 0.00d0 !coeff, power in T 5.695d-5 1.00d0 12 0 !# terms for background gas function: numerator, denominator 456.831d0 3.596417d0 1.0d0 !reducing par for T (= Tc), rho (= Dc), tcx 0.642894d-01 -1.50d0 1.00d0 0.00d0 !coeff, powers of tau=T/Tc (= -power of Tc/T), del, spare for future use -0.530474d-01 -2.00d0 1.00d0 0.00d0 0.453522d-04 -6.00d0 1.00d0 0.00d0 -0.139928d+00 0.00d0 2.00d0 0.00d0 0.166540d+00 -0.50d0 2.00d0 0.00d0 -0.162656d-01 -1.50d0 2.00d0 0.00d0 0.136819d+00 0.00d0 3.00d0 0.00d0 -0.183291d+00 -0.50d0 3.00d0 0.00d0 0.357146d-01 -1.50d0 3.00d0 0.00d0 -0.231210d-01 0.00d0 4.00d0 0.00d0 0.341945d-01 -0.50d0 4.00d0 0.00d0 -0.757341d-02 -1.50d0 4.00d0 0.00d0 TK1 !pointer to critical enhancement auxiliary function #AUX !thermal conductivity critical ehancement model TK1 pure fluid thermal conductivity model of Laesecke et al. (1996) ?LITERATURE REFERENCE\ ?Laesecke, A., Perkins, R.A. and Howley, J.B. (1996). An improved correlation ? for the thermal conductivity of HCFC123 (2,2-dichloro-1,1,1-trifluoroethane). ? Int. J. Refrigeration 19: 231-238.\ ? !end of info section 180.0 !lower temperature limit [K] 480.0 !upper temperature limit [K] 67000.0 !upper pressure limit [kPa] 12.42 !maximum density [mol/L] (= 1900 kg/m^3) 1 0 2 0 !# terms: polynomial-numerator, poly-denom, exp, spare -456.831d0 3.596417d0 1.0d0 !reducing par for T (-Tc indicates tau = Tred/t), rho (= Dc), tcx in polynomial term 0.486742d-02 0.0d0 0.0d0 0.0d0 0.0d0 0 !a13 -456.831d0 3.596417d0 1.0d0 !reducing par for T (-Tc indicates tau = Tred/t), rho (= Dc), tcx in exponential term -100.0d0 -1.0d0 4 0.0d0 0 0 !a14*(tau - 1)**4 -7.08535d0 0.0d0 0 -1.0d0 2 0 !a15*(del - 1)**2 #STN !surface tension specification ST1 surface tension model ?LITERATURE REFERENCE \ ?Okada, M. and Higashi, Y. (1995). "Surface Tension," section 3 in ? R123--Thermodynamic and physical properties, Paris: International Institute ? of Refrigeration.\ ?\ !end info 166.0 !lower temperature limit [K] (Okada lists 237 K, should extrapolate) 456.831 !upper temperature limit [K] 0.00 !(dummy) upper pressure limit 0.00 !(dummy) maximum density 1 !number of terms 456.831d0 !critical temperature used by Okada and Higashi (dummy) 0.05602d0 1.235d0 !sigma0 and n of Okada and Higashi @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890