RE143a !Short name 421-14-7 !CAS number Methyl trifluoromethyl ether !Full name CH3-O-CF3 !Chemical formula {C2H3F3O} HFE-143a !Synonym 100.0398 !Molar mass [g/mol] 240. !Triple point temperature [K] 249.572 !Normal boiling point [K] 377.921 !Critical temperature [K] 3635. !Critical pressure [kPa] 4.648140744 !Critical density [mol/L] 0.289 !Acentric factor 2.48 !Dipole moment [Debye]; (computed by A. Kazakov, Nov. 2017, DF-MP2/def2-QZVPD, unc. 0.1-0.15 D) IIR !Default reference state 10.0 !Version number ???? !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 1S/C2H3F3O/c1-6-2(3,4)5/h1H3 !Standard InChI String :InChi: JRHMNRMPVRXNOS-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: bf6c1a00 !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 E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado ! 12-14-11 EWL, Original version. ! 04-06-13 MLH, Add dipole moment. ! 05-25-16 MLH, Add predictive thermal conductivity, viscosity, and surface tension models. ! 11-15-17 MLH, Revise dipole moment, thermal conductivity, viscosity, and surface tension models based on extremely limited data. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for HFE-143a of Akasaka and Kayukawa (2012). :TRUECRITICALPOINT: 377.921 4.648140744 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1016/j.ijrefrig.2012.01.003 ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Kayukawa, Y., ? "A Fundamental Equation of State for Trifluoromethyl Methyl Ether ? (HFE-143m) and Its Application to Refrigeration Cycle Analysis," ? Int. J. Refrig., 35(4):1003-1013, 2012. doi: 10.1016/j.ijrefrig.2012.01.003 ? ?The uncertainties are 0.1% for liquid density, 0.3% in pressure of the ? vapor phase, and 0.1% for vapor pressure, except in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 240. !Lower temperature limit [K] 420. !Upper temperature limit [K] 7200. !Upper pressure limit [kPa] 12.62 !Maximum density [mol/L] CPP !Pointer to Cp0 model 100.0398 !Molar mass [g/mol] 240. !Triple point temperature [K] 65.35 !Pressure at triple point [kPa] 12.62 !Density at triple point [mol/L] 249.572 !Normal boiling point temperature [K] 0.289 !Acentric factor 377.921 3635.0 4.648140744 !Tc [K], pc [kPa], rhoc [mol/L] 377.921 4.648140744 !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 7.7715884 0.682 1. 0. !a(i),t(i),d(i),l(i) -8.704275 0.851 1. 0. -0.28095049 1.84 1. 0. 0.14540153 1.87 2. 0. 0.0092291277 0.353 5. 0. -0.21416510 3.92 1. 1. 0.099475155 1.14 3. 1. 0.023247135 0.104 5. 1. -0.012873573 1.19 7. 1. -0.057366549 6.58 1. 2. 0.36504650 6.73 2. 2. -0.25433763 7.99 2. 2. -0.090896436 7.31 3. 2. 0.083503619 7.45 4. 2. 0.015477603 16.5 2. 3. -0.016641941 24.8 3. 3. 0.0052410163 10.5 5. 3. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-143a of Akasaka and Kayukawa (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Kayukawa, Y., 2012. ? !``````````````````````````````````````````````````````````````````````````````` 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 20.37 0.0 0.2918 1.0 -0.000195 2.0 4.65e-8 3.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-143a of Akasaka and Kayukawa (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Kayukawa, Y., 2012. ? !``````````````````````````````````````````````````````````````````````````````` 1 5 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 1.4499487026204636 1.0 !ai, ti for [ai*log(tau**ti)] terms -7.5730724565886645 0.0 !aj, ti for [ai*tau**ti] terms 8.0922918999612889 1.0 !aj, ti for [ai*tau**ti] terms 0.0350954850969392 -1.0 -0.234531171827e-04 -2.0 0.559266640510e-08 -3.0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (R134a reference); predictive model for R-E143a. :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** ?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension ? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018. ? doi: 10.6028/NIST.IR.8209 ? ?VISCOSITY ? Extremely limited experimental data found. ? Estimated uncertainty in the gas phase 20%, in the saturated liquid 5%, higher at higher pressures. ? ?THERMAL CONDUCTIVITY ? Extremely limited experimental data found. ? Estimated uncertainty in the gas phase 20%, in the saturated liquid 5%, higher at higher pressures. ? ?The Lennard-Jones parameters were estimated with the method of Chung. ? !``````````````````````````````````````````````````````````````````````````````` 240.0 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 7200.0 !Upper pressure limit [kPa] 12.62 !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) 0.4847 !Lennard-Jones coefficient sigma [nm] from method Chung 300.104 !Lennard-Jones coefficient epsilon/kappa [K] from Chung method 1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.001129 0. 0. 0. !Coefficient, power of T, spare1, spare2 coeff from re245cb 1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.008 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2 0.975 0. 0. 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-E143a of Perkins et al. (2013). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L., ? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids," ? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z ? !``````````````````````````````````````````````````````````````````````````````` 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) 1.02 !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) 0.198e-9 !Xi0 (amplitude) [m] 0.054 !Gam0 (amplitude) [-] 5.88e-10 !Qd_inverse (modified effective cutoff parameter) [m]; R125 value 566.88 !Tref (reference temperature)=1.5*Tc [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for RE143a of Huber (2018). Fit to extrememly limited experimental data. :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension ? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018. ? doi: 10.6028/NIST.IR.8209 ? ?Estimated uncertainty is 10%. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 377.921 !Critical temperature used in fit (dummy) 0.0371 0.98412 !Sigma0 and n 0.0315059 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-E143a of Akasaka and Kayukawa (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 377.921 3635.0 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -7.44314 1.0 1.69164 1.5 -2.27778 2.5 -4.094 5.0 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-E143a of Akasaka and Kayukawa (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 377.921 4.64814 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 1.20552 0.33 1.33568 0.5 0.0981486 1.5 0.248917 2.5 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-E143a of Akasaka and Kayukawa (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 377.921 4.64814 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -3.02576 0.38 -6.97239 1.24 -20.2601 3.2 -53.4441 6.9 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890