R152a !Short name 75-37-6 !CAS number 1,1-Difluoroethane !Full name CHF2CH3 !Chemical formula {C2H4F2} HFC-152a !Synonym 66.051 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 249.127 !Normal boiling point [K] 386.411 !Critical temperature [K] 4516.75 !Critical pressure [kPa] 5.571450 !Critical density [mol/L] 0.27521 !Acentric factor 2.262 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Chem. Eng. Data 36:409-413. IIR !Default reference state 10.0 !Version number 1030 !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 124. !GWP (IPCC 2007) :GWP: 12000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A2 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C2H4F2/c1-2(3)4/h2H,1H3 !Standard InChI String :InChi: NPNPZTNLOVBDOC-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 63f364b0 !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 and S.A. Klein, NIST Thermophysics Division, Boulder, Colorado ! 11-01-95 MM, Original version. ! 11-02-98 EWL, Add Tillner-Roth equation of state. ! 10-06-99 EWL, Fix cp0 part of Tillner-Roth equation of state. ! 11-01-99 EWL, Add Span 12 term short equation of state. ! 01-24-00 EWL, Change transport limits to match EOS. ! 07-09-01 EWL, Add Helmholtz form of BWR equation. ! 11-28-01 MLH, Add viscosity ECS fit as NIST recommended. Kraus ref has asymptote that occurs at approximately 220 K on the liquid sat line. ! 07-05-02 MLH, Change crit model to TK6. ! 09-20-06 EWL, Add Astina and Sato equation. ! 08-17-10 IDC, Add ancillary equations. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ! 01-04-17 MLH, Update critical enhancement model to TK3. ________________________________________________________________________________ #EOS !---Equation of state--- BWR !MBWR equation of state for R-152a of Outcalt and McLinden (1996). :TRUECRITICALPOINT: 386.411 5.57145 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1063/1.555979 ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., ? "A Modified Benedict-Webb-Rubin Equation of State for the Thermodynamic ? Properties of R152a (1,1-Difluoroethane)," ? J. Phys. Chem. Ref. Data, 25(2):605-636, 1996. ? ?The uncertainties of the equation of state are 0.1% in density, 2% in heat ? capacity, and 005% in the vapor speed of sound, except in the critical region. ? The uncertainty in vapor pressure is 0.1%. ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 18.07 !Maximum density [mol/L] CPP !Pointer to Cp0 model 66.051 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 0.06413 !Pressure at triple point [kPa] 18.061 !Density at triple point [mol/L] 249.127 !Normal boiling point temperature [K] 0.27521 !Acentric factor 386.411 4516.75 5.57145 !Tc [K], pc [kPa], rhoc [mol/L] 386.411 5.57145 !Reducing parameters [K, mol/L] 5.57145 !gamma 0.08314471 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term -0.0101623317192 2.15677129618 -64.8581254334 12253.5596303 -2068059.88259 -0.000379836507323 -0.441333232984 158.248874708 564062.216256 -0.000124115350431 0.494972178825 -208.058039834 -0.0131403187106 0.212083848812 -151.263785082 0.0311108025395 -0.00115280979645 0.437040025765 -0.00965596535032 -242705.525346 -51804251.9989 -11907.0545681 459333195.257 -71.9317286511 -8401.0286146 -1.0291095739 -32591.3880841 -0.0041236218223 1.75102808144 -0.19863662464e-4 -0.00421363036104 -1.98696760653 #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-152a of Outcalt & McLinden (1996). ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., 1996. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 1.0 !Reducing parameters for T, Cp0 4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 27.89465 0.0 !C(i), power of T 0.09134686 1.0 0.0002079961 2.0 -2.317613e-7 3.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-152a of Outcalt & McLinden (1996). ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., 1996. ? !``````````````````````````````````````````````````````````````````````````````` 1 5 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 2.3549563857413802 1.0 !ai, ti for [ai*log(tau**ti)] terms -7.9505153063787706 0.0 !aj, ti for [ai*tau**ti] terms 6.870086795465296 1.0 !aj, ti for [ai*tau**ti] terms 0.0109865057017895 -1.0 0.250161892658e-04 -2.0 -0.278744868067e-07 -3.0 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE1 !Helmholtz transformation of MBWR EOS for R-152a of Outcalt and McLinden (1996). ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., ? "A modified Benedict-Webb-Rubin equation of state for the thermodynamic ? properties of R152a (1,1-difluoroethane)," ? J. Phys. Chem. Ref. Data, 25(2):605-636, 1996. doi: 10.1063/1.555979 ? ?The equation here is the same as the Outcalt and McLinden BWR equation, ? but has been transformed into the fundamental Helmholtz energy form. ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 18.07 !Maximum density [mol/L] CPP !Pointer to Cp0 model 66.051 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 0.0641 !Pressure at triple point [kPa] 18.061 !Density at triple point [mol/L] 249.127 !Normal boiling point temperature [K] 0.27521 !Acentric factor 386.411 4516.75 5.57145 !Tc [K], pc [kPa], rhoc [mol/L] 386.411 5.57145 !Reducing parameters [K, mol/L] 8.314471 !Gas constant [J/mol-K] 40 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -3.54657949982 3.0 0. 0. !a(i),t(i),d(i),l(i) -0.36463128062 4.0 0. 0. 0.0333233335558 5.0 0. 0. -0.680968435117 0.0 1. 0. 7.35212646801 0.5 1. 0. -11.2473063838 1.0 1. 0. 5.49916715657 2.0 1. 0. -2.40186327322 3.0 1. 0. -0.0709036447042 0.0 2. 0. -0.213200886814 1.0 2. 0. 0.197839736368 2.0 2. 0. 1.82494769909 3.0 2. 0. -0.0860546479693 0.0 3. 0. 0.88813736654 1.0 3. 0. -0.96612734637 2.0 3. 0. -0.0985223479324 1.0 4. 0. 0.0183419368472 2.0 5. 0. -0.0338550204252 3.0 5. 0. 0.0124921101016 2.0 6. 0. -0.00221056706423 2.0 7. 0. 0.00216879133161 3.0 7. 0. -0.000233597690478 3.0 8. 0. 3.54657949982 3.0 0. 2. 0.36463128062 4.0 0. 2. -0.0333233335558 5.0 0. 2. 2.76133830254 3.0 2. 2. -0.069118571188 4.0 2. 2. -0.0333233335558 5.0 2. 2. 0.782761327717 3.0 4. 2. -0.034559285594 4.0 4. 2. 0.137813531906 5.0 4. 2. 0.186173126153 3.0 6. 2. -0.0341119393297 4.0 6. 2. 0.0459378439687 5.0 6. 2. 0.0216470012607 3.0 8. 2. -0.00852798483242 4.0 8. 2. 0.00620394038634 5.0 8. 2. 0.00185210290813 3.0 10. 2. 0.00101674662734 4.0 10. 2. 0.00124078807727 5.0 10. 2. @EOS !---Equation of state--- FE2 !Helmholtz equation of state for R-152a of Tillner-Roth (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?Tillner-Roth, R., ? "A Fundamental Equation of State for 1,1-Difluoroethane (HFC-152a)," ? Int. J. Thermophys., 16(1):91-100, 1995.doi: 10.1007/BF01438960 ? ?The uncertainties of the equation of state are 0.1% in density, 2% in heat ? capacity, and 005% in the vapor speed of sound, except in the critical region. ? The uncertainty in vapor pressure is 0.1%. ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 435.0 !Upper temperature limit [K] 30000.0 !Upper pressure limit [kPa] 18.03 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 66.051 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 0.065395176 !Pressure at triple point [kPa] 18.020671 !Density at triple point [mol/L] 249.13236 !Normal boiling point temperature [K] 0.26744 !Acentric factor 386.41 4495.0 5.5714524 !Tc [K], pc [kPa], rhoc [mol/L] 386.41 5.5714524 !Reducing parameters [K, mol/L] 8.314471 !Gas constant [J/mol-K] 19 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.355226 0.0 1. 0. !a(i),t(i),d(i),l(i) -1.42566 1.5 1. 0. -0.04631621 3.0 1. 0. 0.06903546 -0.5 1.5 0. 0.0197571 -0.5 3. 0. 0.0007486977 -0.5 6. 0. 0.0004642204 1.5 6. 0. -0.2603396 3.0 1. 1. -0.07624212 4.0 1. 1. 0.2233522 3.0 3. 1. 0.01992515 2.0 4. 1. 0.344904 4.0 1. 2. -0.4963849 5.0 1. 2. 0.1290719 6.0 1. 2. 0.000976079 5.0 8. 2. 0.005066545 12.5 2. 3. -0.0140202 25.0 3. 3. 0.005169918 20.0 5. 3. 0.0002679087 25.0 6. 3. @EOS !---Equation of state--- FES !Helmholtz equation of state for R-152a of Span and Wagner (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Span, R. and Wagner, W. ? "Equations of State for Technical Applications. III. Results for Polar Fluids," ? Int. J. Thermophys., 24(1):111-162, 2003. doi: 10.1023/A:1022362231796 ? ?The uncertainties of the equation of state are approximately 0.2% (to ? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in ? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and ? 0.2% in vapor pressure, except in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 18.1 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 66.051 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 0.064093 !Pressure at triple point [kPa] 18.031 !Density at triple point [mol/L] 249.11 !Normal boiling point temperature [K] 0.275 !Acentric factor 386.41 4519.8 5.5714524 !Tc [K], pc [kPa], rhoc [mol/L] 386.41 5.5714524 !Reducing parameters [K, mol/L] 8.31451 !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 0.95702326 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.3707196 1.25 1. 0. 0.18748463 1.5 1. 0. 0.063800843 0.25 3. 0. 0.00016625977 0.875 7. 0. 0.082208165 2.375 1. 1. 0.57243518 2.0 2. 1. 0.0039476701 2.125 5. 1. -0.23848654 3.5 1. 2. -0.080711618 6.5 1. 2. -0.073103558 4.75 4. 2. -0.015538724 12.5 2. 3. @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for R-152a. ? ?``````````````````````````````````````````````````````````````````````````````` ?Tillner-Roth, R., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314471 !Reducing parameters for T, Cp0 3 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 1.4652739 0.25 0.00002627677 2.0 -0.29988241e-10 4.0 @EOS !---Equation of state--- FE3 !Helmholtz equation of state for R-152a of Astina and Sato (2004). ? ?``````````````````````````````````````````````````````````````````````````````` ?Astina, I.M. and Sato, H., ? "A Rigorous Thermodynamic Property Model for Fluid-Phase ? 1,1-Difluoroethane (R-152a)," ? Int. J. Thermophys., 25(6):1713-1733, 2004. doi: 10.1007/s10765-004-7731-8 ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 450.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 18.04 !Maximum density [mol/L] PH3 !Pointer to Cp0 model 66.050 !Molar mass [g/mol] 154.56 !Triple point temperature [K] 0.064 !Pressure at triple point [kPa] 18.04 !Density at triple point [mol/L] 249.117 !Normal boiling point temperature [K] 0.275 !Acentric factor 386.41 4516.0 5.571536715 !Tc [K], pc [kPa], rhoc [mol/L] 386.41 5.571536715 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 17 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 1.753847317 0.5 1. 0. !a(i),t(i),d(i),l(i) -4.049760759 1.125 1. 0. -0.2277389257 2.875 1. 0. 0.708775195 0.875 2. 0. -0.5528619502 1.875 2. 0. -0.03025046686 0.5 3. 0. 0.1396289974 1.875 3. 0. 1.121238954e-4 4.0 4. 0. 1.181005890 1.25 1. 1. 1.535785579 2. 2. 1. 0.7468363045 2.75 3. 1. -0.1252266405 6.0 1. 2. -0.03898223986 9.0 2. 2. -0.07260588801 6.0 3. 2. -0.00265930225 22.0 3. 3. 0.004210849329 20.0 4. 3. 2.015953966e-4 32.0 5. 3. @AUX !---Auxiliary function for PH0 PH3 !Helmholtz form for the ideal-gas state ? ?``````````````````````````````````````````````````````````````````````````````` ?Astina, I.M. and Sato, H. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 4 2 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh -1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms -9.508135074 0.0 !aj, ti for [ai*tau**ti] terms 6.812068779 1.0 -7.285916044 -0.5 6.741130104 0.25 1.978152028 -1.753741145 5.880826311 -4.360150337 ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for R-152a of Krauss et al. (1996). :DOI: 10.1007/BF01439187 ? ?``````````````````````````````````````````````````````````````````````````````` ?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K., ? "Transport Properties of 1,1-Difluoroethane (R152a)," ? Int. J. Thermophys., 17:731-757, 1996. doi: 10.1007/BF01439187 ? ?The uncertainty in thermal conductivity is 3% in the dilute gas and 5% ? elsewhere (10% in the critical region). ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] !Krauss claims only 240 K, but seems to extrapolate fine 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 18.07 !Maximum density [mol/L] 2 0 !# terms for dilute gas function: numerator, denominator 1.0 0.001 !Reducing parameters for T, tcx [Krauss corr in mW/m.K] -14.942 0. !Coefficient, power in T 0.0973283 1. 4 0 !# terms for background gas function: numerator, denominator 1.0 5.57145 0.001115 !Reducing parameters for T, rho (rho_c), tcx 9.1809 0. 1. 0. !Coefficient, powers of T, rho, spare for future use 11.8577 0. 2. 0. -5.4473 0. 3. 0. 1.71379 0. 4. 0. TK3 !Pointer to critical enhancement auxiliary function #AUX !---Auxiliary function for the thermal conductivity critical enhancement TK3 !Simplified thermal conductivity critical enhancement for R-152a 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: 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) 1.075 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1) 0.1894e-9 !Xi0 (amplitude) [m] 0.0487 !Gam0 (amplitude) [-] 4.37e-10 !Qd_inverse (modified effective cutoff parameter) [m] 579.617 !Tref (reference temperature) [= 1.5 * 386.411 K] ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); fitted to data for R-152a. :DOI: 10.1016/S0140-7007(96)00073-4 ? ?``````````````````````````````````````````````````````````````````````````````` ?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4. ?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9 ? ?VISCOSITY ? The ECS parameters for viscosity were based on the data of: ? vanderGulik, P. S.(1995)"Viscosity of saturated R152a measured with a vibrating wire viscometer" Int. J. Thermophys.,16, 867-76 doi: 10.1007/BF02093469 ? Takahashi, M., Yokoyama, C., and Takahashi, S.(1987)"Viscosities of Gaseous R13B1, R142b, and R152a" J. Chem. Eng. Data,32,98-103. doi: 10.1021/je00047a027 ? Assael, M. J., Polimatidou, S. K., Vogel, E., and Wakeham, W. A.(1994). "Measurements of the viscosity of R11, R12, R141b, and R152a in the temperature range 270-340 K at pressures up to 20 MPa" Int. J. Thermophys.,15,575-89. ? Karbanov, E.M. (1978). "Investigation of the Dynamic Viscosity of Some Freons of Ethane Type and of the Bromide Freons" Ph.D. Thesis, Groz. Neft. Inst., Grozny, USSR ? Average absolute deviations of the fit from the experimental data are: ? vanderGulik: 4.77%; Takahashi: 1.73%; Assael: 1.62%; Karbanov:5.64% ? Overall: 2.78% ? ?The Lennard-Jones parameters were taken from Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K., "Transport properties of 1,1-Difluoroethane (R152a),"Int. J. Thermophysics 17:731-757, 1996. ? !``````````````````````````````````````````````````````````````````````````````` 154.56 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 18.07 !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) 0.46115 !Lennard-Jones coefficient sigma [nm] for ECS method 354.84 !Lennard-Jones coefficient epsilon/kappa [K] for ECS 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 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 0.824547 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 0.0640641 0. 1. 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 ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-152a 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 386.411 !Critical temperature used in fit (dummy) 0.05808 1.2115 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-152a 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. ! 386.411 4516.75 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.4821 1.0 2.1105 1.5 -2.0761 2.2 -3.5539 4.8 0.58004 6.2 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-152a 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. ! 386.411 5.571536715 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 19.914 0.56 -68.624 0.76 99.821 0.95 -77.984 1.20 29.913 1.40 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-152a 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. ! 386.411 5.571536715 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -3.3621 0.406 -8.5985 1.42 -2.6830 3.6 -24.140 3.9 -43.159 8.0 -28.045 9.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890 @ETA !Viscosity model specification VS1 pure fluid viscosity model of Krauss et al. (1996). ? ?``````````````````````````````````````````````````````````````````````````````` ?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K., ? "Transport properties of 1,1-Difluoroethane (R152a)," ? Int. J. Thermophysics 17:731-757, 1996. ? ?The uncertainty in viscosity is 1% in the dilute gas, and 3% elsewhere above ? 300 K. ? !``````````````````````````````````````````````````````````````````````````````` 240.0 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 15.90 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI1 !Pointer to reduced effective collision cross-section model 0.46115 !Lennard-Jones coefficient sigma [nm] 354.84 !Lennard-Jones coefficient epsilon/kappa [K] 1.0 1.0 !Reducing parameters for T, eta 0.2169614 0.5 !Chapman-Enskog term 0 !Number of terms for initial density dependence 0 5 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential 1.0 5.571537 51.12 !Reducing parameters for T, rho (= 368 kg/m^3, note: Krauss uses MW = 66.05), eta (= the pseudo-critical viscosity) -0.139987 0.0 0. 0. 0 ! E5*E6; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present] -0.0737927 0.0 1. 0. 0 ! E1 0.517924 0.0 2. 0. 0 ! E2 -0.308875 0.0 3. 0. 0 ! E3 0.108049 0.0 4. 0. 0 ! E4 -0.408387 0.0 0. 0. 0 ! E5 -2.91733 0.0 0. 0. 0 ! -E6 term in denominator 1.0 0.0 1. 0. 0 !Rho/rhoc term in denominator NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) #AUX !---Auxiliary function for the collision integral CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for R-152a. ? ?``````````````````````````````````````````````````````````````````````````````` ?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K., ? "Transport properties of 1,1-Difluoroethane (R152a)," ? Int. J. Thermophysics 17:731-757, 1996. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 5 !Number of terms 0.4425728 0 !Coefficient, power of Tstar -0.5138403 1 0.1547566 2 -0.02821844 3 0.001578286 4