R11 !Short name 75-69-4 !CAS number Trichlorofluoromethane !Full name CCl3F !Chemical formula {CCl3F} CFC-11 !Synonym 137.368 !Molar mass [g/mol] 162.68 !Triple point temperature [K] 296.858 !Normal boiling point [K] 471.11 !Critical temperature [K] 4407.638 !Critical pressure [kPa] 4.032962 !Critical density [mol/L] 0.18875 !Acentric factor 0.450 !Dipole moment [Debye]; value from REFPROP v5.0 IIR !Default reference state 10.0 !Version number ???? !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 4750. !GWP (IPCC 2007) :GWP: 1.0 !ODP (WMO 2010) :ODP: 1100. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/CCl3F/c2-1(3,4)5 !Standard InChI String :InChi: CYRMSUTZVYGINF-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 6f9b71e0 !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 ! 01-31-96 MM, Original version. ! 11-01-99 EWL, Add Span 12 term short equation of state. ! 11-01-99 EWL, Add Marx et al. equation of state. ! 11-13-06 MLH, Add LJ parameters. ! 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-11 of Jacobsen et al. (1992). :TRUECRITICALPOINT: 471.11 4.032962 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1016/0378-3812(92)87054-Q ? ?``````````````````````````````````````````````````````````````````````````````` ?Jacobsen, R.T, Penoncello, S.G., and Lemmon, E.W., ? "A Fundamental Equation for Trichlorofluoromethane (R-11)," ? Fluid Phase Equilib., 80:45-56, 1992. ? ?The uncertainties of the equation of state are 0.1% in density for the liquid, ? and 0.25% for the vapor, 2% in heat capacity, and 1% in the speed of sound, ? except in the critical region. The uncertainty in vapor pressure is 0.2%. ? !``````````````````````````````````````````````````````````````````````````````` 162.68 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 30000.0 !Upper pressure limit [kPa] 12.88 !Maximum density [mol/L] CPP !Pointer to Cp0 model 137.368 !Molar mass [g/mol] 162.68 !Triple point temperature [K] 0.006510 !Pressure at triple point [kPa] 12.8745 !Density at triple point [mol/L] 296.858 !Normal boiling point temperature [K] 0.18875 !Acentric factor 471.11 4407.638 4.032962 !Tc [K], pc [kPa], rhoc [mol/L] 471.11 4.032962 !Reducing parameters [K, mol/L] 8.314510 !Gas constant [J/mol-K] 28 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 1.25993633881 0.5 1. 0. !a(i),t(i),d(i),l(i) -2.60818574641 1.5 1. 0. 0.00982122542463 5.0 1. 0. -1.06085385839 1.0 2. 0. 1.2282036351 1.5 2. 0. 0.118000776439 0.0 3. 0. -0.000698956926463 5.0 3. 0. -0.0355428373358 2.0 4. 0. 0.00197169579643 3.0 4. 0. -0.00848363012252 1.0 5. 0. 0.00417997567653 2.0 5. 0. -0.000242772533848 4.0 5. 0. 0.00313371368974 1.0 6. 0. 0.396182646586e-5 4.0 8. 0. 0.339736319502 5.0 1. 2. -0.203010634531 6.0 1. 2. -0.1060178599 3.5 2. 2. 0.45156488259 5.5 2. 2. -0.339265767612 7.5 2. 2. 0.114338523359 3.0 3. 2. 0.0319537833995 2.5 4. 2. 0.036790825978 5.0 6. 2. -0.961768948364e-5 1.5 10. 2. 0.00246717966418 11.0 3. 4. -0.00167030256045 9.0 5. 6. 0.00240710110806 13.0 8. 6. 0.00156214678738 5.0 9. 6. -0.00323352596704 9.0 9. 6. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-11 of Jacobsen et al. (1992). ? ?``````````````````````````````````````````````````````````````````````````````` ?Jacobsen, R.T, Penoncello, S.G., and Lemmon, E.W., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31451 !Reducing parameters for T, Cp0 2 6 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.00564923 0.0 ! = 4 + A11/R (the Ai are coeff of Jacobsen) 0.0002228875 1.0 ! = A12/R 1.0 1561.076 ! = A1*A1 2.0 1218.647 ! = A2*A1 (degenerate mode--taken twice) 1.0 770.035 ! = A4*A1 2.0 572.634 ! = A5*A1 (degenerate mode--taken twice) 1.0 502.854 ! = A7*A1 2.0 346.746 ! = A8*A1 (degenerate mode--taken twice) #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-11 of Jacobsen et al. (1992). ? ?``````````````````````````````````````````````````````````````````````````````` ?Jacobsen, R.T, Penoncello, S.G., and Lemmon, E.W., ? !``````````````````````````````````````````````````````````````````````````````` 1 3 6 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 3.00564923 1.0 !ai, ti for [ai*log(tau**ti)] terms -17.7938110160538514 0.0 !aj, ti for [ai*tau**ti] terms 10.0839710927509554 1.0 !aj, ti for [ai*tau**ti] terms 0.0002228875 -1.0 1.0 1561.076 !aj, ti for [ai*log(1-exp(-ti/T)] terms 2.0 1218.647 1.0 770.035 2.0 572.634 1.0 502.854 2.0 346.746 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE1 !Helmholtz equation of state for R-11 of Marx et al. (1992). ? ?``````````````````````````````````````````````````````````````````````````````` ?Marx, V., Pruss, A., and Wagner, W., ? "New Equation of State for R 12, R 22, R 11 and R 113," ? Fortschr.-Ber. VDI, Dusseldorf: VDI-Verlag, 19(57), 1992. ? !``````````````````````````````````````````````````````````````````````````````` 162.68 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 30000.0 !Upper pressure limit [kPa] 13.0 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 137.36803 !Molar mass [g/mol] 162.68 !Triple point temperature [K] 0.0066057 !Pressure at triple point [kPa] 12.945 !Density at triple point [mol/L] 296.79 !Normal boiling point temperature [K] 0.18808 !Acentric factor 471.06 4393.5 4.113039 !Tc [K], pc [kPa], rhoc [mol/L] 471.06 4.113039 !Reducing parameters [K, mol/L] 8.31451 !Gas constant [J/mol-K] 21 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -2.19644325 1.5 1. 0. !a(i),t(i),d(i),l(i) 0.8562148696 2.0 1. 0. 0.0185864982 3.0 1. 0. 0.2807246052 0.0 2. 0. -0.08526398864 1.5 3. 0. 0.01090334698 1.0 5. 0. 0.4138515982 -0.5 1. 1. -0.3125498519 3.5 1. 1. 0.1545749737 -0.5 2. 1. 0.1752299625 1.0 3. 1. 0.02295443969 -0.5 5. 1. -0.002094422944 2.0 7. 1. -0.1267942875e-8 4.0 14. 1. 0.00797272861 8.0 1. 2. -0.1520330549 8.0 2. 2. 0.06448637628 8.0 3. 2. 0.0002046144277 4.0 11. 2. -0.4100829613e-4 6.0 11. 2. -0.0123188575 18.0 4. 3. 0.006681486552 21.0 4. 3. -0.6742271171e-7 33.0 10. 4. @EOS !---Equation of state--- FES !Helmholtz equation of state for R-11 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. ? !``````````````````````````````````````````````````````````````````````````````` 162.68 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 13.0 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 137.368 !Molar mass [g/mol] 162.68 !Triple point temperature [K] 0.0066915 !Pressure at triple point [kPa] 12.963 !Density at triple point [mol/L] 296.81 !Normal boiling point temperature [K] 0.187 !Acentric factor 471.06 4393.5 4.1130394 !Tc [K], pc [kPa], rhoc [mol/L] 471.06 4.1130394 !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 1.0656383 0.25 1. 0. !a(i),t(i),d(i),l(i) -3.2495206 1.25 1. 0. 0.87823894 1.5 1. 0. 0.087611569 0.25 3. 0. 0.00029950049 0.875 7. 0. 0.42896949 2.375 1. 1. 0.70828452 2.0 2. 1. -0.017391823 2.125 5. 1. -0.37626521 3.5 1. 2. 0.011605284 6.5 1. 2. -0.089550567 4.75 4. 2. -0.030063991 12.5 2. 3. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for R-11. ? ?``````````````````````````````````````````````````````````````````````````````` ?Marx, V., Pruss, A., and Wagner, W., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31451 !Reducing parameters for T, Cp0 1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0000024 0.0 3.2960961 381.63168 2.8401126 1368.22648 0.40350474 3435.66931 3.0739271 689.55053 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (R134a reference); fitted to data for R-11. :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. Refrig., 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. Refrig., 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9 ? ?THERMAL CONDUCTIVITY ? The ECS parameters for thermal conductivity were based on the data of: ? Richard, R.G. and Shankland, I.R., "A Transient Hot-Wire Method for Measuring the Thermal Conductivity of Gases and Liquids," Int. J. Thermophys., 10:673-686, 1989. doi: 10.1007/BF00507988 ? Shankland, I.R., "Transport Properties of CFC Alternatives," paper presented at AIChE Spring National Meeting, Orlando, Florida, 1990. ? Yata, J., Minamiyama, T., and Tanaka, S., "Measurement of Thermal Conductivity of Liquid Fluorocarbons," Int. J. Thermophys., 5:209-218, 1984. doi: 10.1007/BF00505501 ? Average absolute deviations of the fit from the experimental data are: ? Richard: 1.19%; Shankland: 0.96%; Yata: 1.16%. Overall: 1.08%. ? ?VISCOSITY ? The ECS parameters for viscosity were based on the data of: ? Assael, M.J., Polimatidou, S.K., Vogel, E., and Wakeham, W.A., " 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(4):575-589, 1994. doi: 10.1007/BF01563788 ? Kumagai, A. and Takahashi, S., "Viscosity of Saturated Liquid Fluorocarbon Refrigerants from 273 to 353 K," Int. J. Thermophys., 12(1):105-117, 1991. doi: 10.1007/BF00506125 ? Nagashima, A., Harada, J., and Tanishita, I., "Viscosity of Halogenated Refrigerants: 1st Report, Measurement of Liquid R11," Transactions of the Japan Society of Mechanical Engineers, 41(342):656-661, 1975. doi: 10.1299/kikai1938.41.656 ? Average absolute deviations of the fit from the experimental data are: ? Assael: 1.18%; Kumagai: 0.66%; Nagashima: 1.12%. Overall: 1.10%. ? ?The Lennard-Jones parameters were estimated from corresponding states with R134a and 298 K as a reference. ? !``````````````````````````````````````````````````````````````````````````````` 162.68 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 30000.0 !Upper pressure limit [kPa] 12.88 !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) 0.5447 !Lennard-Jones coefficient sigma [nm] for ECS method 363.609 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.0014 0. 0. 0. !Coefficient, power of T, spare1, spare2 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.0653851 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0250121 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 1.0724 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.022672 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare NUL !Pointer to critical enhancement auxiliary function ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-11 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 471.11 !Critical temperature used in fit (dummy) 0.06212 1.247 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-11 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. ! 471.11 4407.638 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.0742 1.0 3.8118 1.5 -3.2850 1.73 -7.6340 5.2 5.0598 6.0 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-11 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. ! 471.11 4.032962 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 2.0368 0.357 12.850 1.5 -22.521 1.7 11.340 2.0 -0.94375 3.0 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-11 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. ! 471.11 4.032962 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -3.0296 0.417 -6.0723 1.25 -15.890 3.1 -63.024 6.8 87.167 10.0 -157.15 12.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890