R1234ze(Z) !Short name 29118-25-0 !CAS number cis-1,3,3,3-Tetrafluoropropene !Full name CHF=CHCF3 (cis) !Chemical formula {C3F4H2} R-1234ze(Z) !Synonym 114.0416 !Molar mass [g/mol] 238. !Triple point temperature [K] (currently set at Tlow, not Ttrp) 282.878 !Normal boiling point [K] 423.27 !Critical temperature [K] 3530.6 !Critical pressure [kPa] 4.0 !Critical density [mol/L] 0.327 !Acentric factor 2.9 !Dipole moment [Debye]; (computed 10/17 by A. Kazakov, NIST, 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: ???? !GWP :GWP: 1S/C3H2F4/c4-2-1-3(5,6)7/h1-2H/b2-1- !Standard InChI String :InChi: CDOOAUSHHFGWSA-UPHRSURJSA-N !Standard InChI Key :InChiKey: 9905ef70 (R1234ze(E)) !Alternative fluid for mixing rules :AltID: e23fd030 !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 ! 12-17-13 EWL, Original version. ! 07-07-14 MLH, Add predictive transport. ! 03-09-15 EWL, Add surface tension equation of Kondou et al. (2015). ! 02-16-17 KG, Add ancillary equations. ! 08-24-17 RA, Add final equation of state of Akasaka and Lemmon (2018). ! 10-20-17 MLH, Add dipole moment, revise predictive transport ! 01-12-17 MLH, Add new ECS transport based on preliminary data from Miyara (2018). ! 02-05-18 RA, Add ancillary equations. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for R-1234ze(Z) of Akasaka and Lemmon (2018). :TRUECRITICALPOINT: 423.27 4.0 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Lemmon, E.W., ? "Fundamental Equations of State for cis-1,3,3,3-Tetrafluoropropene (R-1234ze(Z)) ? and 3,3,3-Trifluoropropene (R-1243zf)," ? to be submitted to J. Chem. Eng. Data, 2018. ? ?Typical uncertainties over the range of validity are 0.1% for vapor pressures at ? temperatures above 300 K, 0.3% for those at lower temperatures, 0.1% for liquid ? densities, and 0.3% for vapor densities, except in the critical region where ? larger deviations up to about 1% are observed in densities. The uncertainties ? in sound speeds are 0.02% in the vapor phase and 0.05% in the liquid phase. ? !``````````````````````````````````````````````````````````````````````````````` 238. !Lower temperature limit [K] 440.0 !Upper temperature limit [K] 34000.0 !Upper pressure limit [kPa] 12.01 !Maximum density [mol/L] CPP !Pointer to Cp0 model 114.0416 !Molar mass [g/mol] 238. !Triple point temperature [K] (currently set at Tlow, not Ttrp) 11.942 !Pressure at triple point [kPa] 12.01 !Density at triple point [mol/L] 282.878 !Normal boiling point temperature [K] 0.327 !Acentric factor 423.27 3530.6 4.0 !Tc [K], pc [kPa], rhoc [mol/L] 423.27 4.0 !Reducing parameters [K, mol/L] 8.3144598 !Gas constant [J/mol-K] 10 4 6 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.03194509 1. 4. 0. !a(i),t(i),d(i),l(i) 1.394592 0.333 1. 0. -2.300799 1. 1. 0. -0.2556693 1. 2. 0. 0.1282934 0.38 3. 0. -1.335381 2.85 1. 2. -1.366494 3.16 3. 2. 0.2004912 0.607 2. 1. -0.6489709 2.2 2. 2. -0.02220033 1. 7. 1. 1.66538 1.83 1. 2. 2. -1.108 -0.563 1.246 0.933 0. 0. 0. 0.3427048 3.3 1. 2. 2. -1.579 -1.724 1.05 0.786 0. 0. 0. -0.6510217 1.9 3. 2. 2. -1.098 -0.806 1. 0.496 0. 0. 0. -0.5067066 2.6 2. 2. 2. -0.672 -0.505 0.677 0.327 0. 0. 0. -0.1231787 2.9 3. 2. 2. -3.38 -26.4 1.302 0.523 0. 0. 0. 0.08828106 3. 2. 2. 2. -1.6 -8.82 1.274 0.308 0. 0. 0. eta beta gamma epsilon EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2] #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-1234ze(Z) of Akasaka and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Lemmon, E.W., 2018. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.3144598 !Reducing parameters for T, Cp0 1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0 0.0 4.2365 20.0 13.063 1335.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-1234ze(Z) of Akasaka and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R. and Lemmon, E.W., 2018. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 2 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 -2.422442259289312 0.0 !aj, ti for [ai*tau**ti] terms 8.1905398438971062 1.0 !aj, ti for [ai*tau**ti] terms 4.2365 20.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 13.063 1335.0 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE1 !Helmholtz equation of state for R-1234ze(Z) of Akasaka et al. (2014). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., Higashi, Y., Miyara, A., Koyama, S. ? "A Fundamental Equation of State for Cis-1,3,3,3-tetrafluoropropene (R-1234ze(Z))," ? Int. J. Refrig., 44, 168-176 (2014). 10.1016/j.ijrefrig.2013.12.018 ? ?The estimated uncertainties of properties calculated from the equation are ? 0.15 % in vapor pressures, 0.4 % in vapor densities, 0.2 % in liquid densities, ? and 0.05 % in the vapor phase sound speeds. ? !``````````````````````````````````````````````````````````````````````````````` 273.0 !Lower temperature limit [K] 430.0 !Upper temperature limit [K] 6000.0 !Upper pressure limit [kPa] 11.26 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 114.0416 !Molar mass [g/mol] 273. !Triple point temperature [K] (currently set at Tlow, not Ttrp) 67.8 !Pressure at triple point [kPa] 11.26 !Density at triple point [mol/L] 282.895 !Normal boiling point temperature [K] 0.3274 !Acentric factor 423.27 3533.0 4.1267 !Tc [K], pc [kPa], rhoc [mol/L] 423.27 4.1267 !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 7.7652368 0.685 1. 0. -8.7025756 0.8494 1. 0. -0.28352251 1.87 1. 0. 0.14534501 2. 2. 0. 0.0092092105 0.142 5. 0. -0.24997382 4.2 1. 1. 0.09667436 0.08 3. 1. 0.024685924 0.0 5. 1. -0.013255083 1.1 7. 1. -0.06423133 5.5 1. 2. 0.36638206 6.6 2. 2. -0.25548847 8.4 2. 2. -0.095592361 7.2 3. 2. 0.086271444 7.6 4. 2. 0.015997412 8.5 2. 3. -0.013127234 23.0 3. 3. 0.004229399 18.0 5. 3. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for R-1234ze(Z) of Akasaka et al. (2014). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., Higashi, Y., Miyara, A., Koyama, S. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 423.27 8.314472 !Reducing parameters for T, Cp0 4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh -1.6994 0.0 24.527 1.0 -9.9249 2.0 1.5158 3.0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (R134a reference) for R-1234ze(Z). :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 ? ?Fits based on fit of preliminary unpublished data of Miyara, Saga University, Japan, 2018. ? Uncertainty for viscosity in the saturated liquid phase is 3%, 4% for vapor over 300 to 450 K, higher at higher pressures. ? Uncertainty for thermal conductivity in the saturated liquid phase is 2%, 3% for vapor over 300 to 430 K, higher near critical and at higher pressures. ? ?The Lennard-Jones parameters were estimated with the method of Chung. ? !``````````````````````````````````````````````````````````````````````````````` 238. !Lower temperature limit [K] 440.0 !Upper temperature limit [K] 34000.0 !Upper pressure limit [kPa] 12.01 !Maximum density [mol/L] FEQ R134A.FLD VS1 !Model for reference fluid viscosity TC1 !Model for reference fluid thermal conductivity BIG !Large molecule identifier 0.85 0. 0. 0. !Large molecule parameters 1 !Lennard-Jones flag (0 or 1) (0 => use estimates) 0.5096 !Lennard-Jones coefficient sigma [nm] 336.11 !Lennard-Jones coefficient epsilon/kappa [K] 1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.00162 0. 0. 0. !Coefficient, power of T, spare1, spare2 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 0.829337 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 0.0476201 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 1.10592 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0471388 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-1234ze(Z) 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: 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) 0.206e-9 !Xi0 (amplitude) [m] 0.055 !Gam0 (amplitude) [-] 0.620e-9 !Qd_inverse (modified effective cutoff parameter) [m] 634.91 !Tref (reference temperature) [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-1234ze(Z) of Kondou et al. (2015). :DOI: 10.1016/j.ijrefrig.2015.01.005 ? ?``````````````````````````````````````````````````````````````````````````````` ?Kondou, C., Nagata, R., Nii, N., Koyama, S., and Higashi, Y., ? "Surface Tension of Low GWP Refrigerants R1243zf, R1234ze(Z), and R1233zd(E)," ? Int. J. Refrig., 53:80-89, 2015. ? doi: 10.1016/j.ijrefrig.2015.01.005 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 423.27 !Critical temperature used in fit (dummy) 0.05657 1.22 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-1234ze(Z) of Akasaka (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., 2018. ? ?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. ! 423.27 3530.6 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -7.7093 1.0 2.3374 1.5 -2.1124 2.0 -3.1074 4.2 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-1234ze(Z) of Akasaka (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., 2018. ? ?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. ! 423.27 4.0 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 1.3241 0.265 2.3135 0.75 -1.2904 1.3 0.67545 1.95 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-1234ze(Z) of Akasaka (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., 2018. ? ?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. ! 423.27 4.0 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -1.9019 0.3 -6.4503 0.96 -15.730 2.7 -47.277 5.8 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890