613 lines
30 KiB
Plaintext
613 lines
30 KiB
Plaintext
R161 !Short name
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353-36-6 !CAS number
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Fluoroethane !Full name
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C2H5F !Chemical formula {C2H5F}
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Ethyl fluoride !Synonym
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48.0595 !Molar mass [g/mol]
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130.0 !Triple point temperature [K]
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235.614 !Normal boiling point [K]
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375.25 !Critical temperature [K]
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5046.0 !Critical pressure [kPa]
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6.2839 !Critical density [mol/L]
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0.220 !Acentric factor
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1.9397 !Dipole moment [Debye]; Nelson, R.D., Lide, D.R., Maryott, A., NSRDS10, NBS,(1967).
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IIR !Default reference state
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10.0 !Version number
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2453 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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1S/C2H5F/c1-2-3/h2H2,1H3 !Standard InChI String :InChi:
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UHCBBWUQDAVSMS-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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edb53660 !Hash number from InChI Key :Hash:
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!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
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! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
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! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
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! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
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! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
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! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
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! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
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! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
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! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
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! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
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! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
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! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
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! end of the fluid file is marked with @END. Anything below that is ignored.
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! compiled by E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 03-02-05 EWL, Original version.
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! 01-27-10 MLH, Add predictive transport.
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! 02-08-10 MM, Add surface tension based on the homologous series ethane (C2H6) through R116 (C2F6).
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! 09-01-10 EWL, Add ancillary equations.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 03-13-13 EWL, Add equation of state of Wu and Zhou (2012).
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! 03-23-16 EWL, Add equation of state of Qi et al. (2016).
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! 06-02-16 MLH, Revise ECS transport with fit to available data.
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! 01-11-17 MLH, Add Tsolakidou et al. (2017) thermal conductivity and viscosity formulations.
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! 02-16-17 KG, Add ancillary equations.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-161 of Qi et al. (2016).
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:TRUECRITICALPOINT: 375.25 6.2839 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
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:DOI: 10.1007/s10765-011-1151-3
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Qi, H., Fang, D., Gao, K., Meng, X., and Wu, J.,
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? "Compressed Liquid Densities and Helmholtz Energy Equation of State for
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? Fluoroethane (R161),"
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? Int. J. Thermophys., 37:55, 2016.
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? doi: 10.1007/s10765-016-2061-1
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?
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?The estimated uncertainties of properties are estimated to be 0.25 % in
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? density, 0.2 % in saturated liquid density between 230 K and 320 K, and 0.2 % in
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? vapor pressure below 350 K. Deviations in the critical region are higher for all
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? properties. The extrapolation behavior of the new formulation at high
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? temperatures and high pressures is reasonable.
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?
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!```````````````````````````````````````````````````````````````````````````````
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130.0 !Lower temperature limit [K]
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450.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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19.95 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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48.0595 !Molar mass [g/mol]
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130.0 !Triple point temperature [K]
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0.005941 !Pressure at triple point [kPa]
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19.95 !Density at triple point [mol/L]
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235.614 !Normal boiling point temperature [K]
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0.220 !Acentric factor
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375.25 5046.0 6.2839 !Tc [K], pc [kPa], rhoc [mol/L] (218.5 kg/m^3)
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375.25 6.2839 !Reducing parameters [K, mol/L]
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8.3144598 !Gas constant [J/mol-K]
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12 4 6 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.005145283 1.0 5. 0. !a(i),t(i),d(i),l(i)
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-0.001882274 0.68 4. 0.
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1.884722 0.32 1. 0.
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-3.1819965 0.92 1. 0.
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-0.24432415 1.23 2. 0.
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0.27792467 0.846 3. 0.
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-0.4414064 4.208 1. 2.
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-0.402065 3.06 3. 2.
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0.24171113 1.85 2. 1.
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-0.16603585 4.28 2. 2.
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-0.03440867 1.003 7. 1.
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-0.000099185 1.12 5. 1.
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1.0146668 1.055 1. 2. 2. -0.96212 -0.62848 1.9363 0.70192 0. 0. 0.
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-0.03542609 0.8 1. 2. 2. -3.2147 -4.5968 1.5054 1.23824 0. 0. 0.
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-0.006038245 4.08 3. 2. 2. -2.6288 -4.9696 1.3691 0.73324 0. 0. 0.
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-0.025437558 1.6 3. 2. 2. -0.8657 -0.239 2.3594 0.6258 0. 0. 0.
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-0.00515678 3.85 2. 2. 2. -2.3839 -0.788 0.5581 1.564 0. 0. 0.
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0.006396804 0.57 2. 2. 2. -1.7814 -7.0874 0.6326 1.4861 0. 0. 0.
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eta beta gamma epsilon
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EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-161 of Qi et al. (2016).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Qi, H., Fang, D., Gao, K., Meng, X., and Wu, J., 2016.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.3144598 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0 0.0
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1.08888 329.0
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1.80842 742.0
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8.72417 1644.0
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5.67715 3922.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-161 of Qi et al. (2016).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Qi, H., Fang, D., Gao, K., Meng, X., and Wu, J., 2016.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-6.9245844727154946 0.0 !aj, ti for [ai*tau**ti] terms
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5.4918186246971583 1.0 !aj, ti for [ai*tau**ti] terms
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1.08888 329.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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1.80842 742.0
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8.72417 1644.0
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5.67715 3922.0
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for R-161 of Wu and Zhou (2012).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Wu, J. and Zhou, Y.,
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? "An Equation of State for Fluoroethane (R161),"
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? Int. J. Thermophys. 33:220-234, 2012. doi: 10.1007/s10765-011-1151-3
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?
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?As there are very few compressed liquid-density experimental data published, the
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? uncertainties in density of the equation of state are estimated to be 2.0% in
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? the compressed-liquid region and 0.5% in the gas and supercritical regions.
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? Uncertainties in vapor pressure are 0.5% above 200 K and increase at lower
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? temperatures. The uncertainties for all properties are higher in the critical
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? region, except vapor pressure.
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?
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!```````````````````````````````````````````````````````````````````````````````
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130.0 !Lower temperature limit [K]
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450.0 !Upper temperature limit [K]
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5000.0 !Upper pressure limit [kPa]
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20.0 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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48.0595 !Molar mass [g/mol]
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130.0 !Triple point temperature [K]
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0.005512 !Pressure at triple point [kPa]
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19.91 !Density at triple point [mol/L]
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235.6 !Normal boiling point temperature [K]
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0.216 !Acentric factor
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375.25 5010.0 6.28 !Tc [K], pc [kPa], rhoc [mol/L] (218.5 kg/m^3)
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375.25 6.28 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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10 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.04133 1.0 4. 0. !a(i),t(i),d(i),l(i)
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1.511 0.37 1. 0.
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-2.3 0.97 1. 0.
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-0.457 1.14 2. 0.
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0.1683 0.744 3. 0.
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0.62187 1.26 2. 1.
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-0.0265 1. 7. 1.
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-1.03 1.8 1. 2.
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-0.285 3. 2. 2.
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-0.476 2.25 3. 2.
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0.82 1. 1. 2. 2. -0.96 -2.7 0.9 0.683 0. 0. 0.
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-0.3532 1.2 1. 2. 2. -1.35 -5.2 0.69 0.892 0. 0. 0.
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-0.116 5.3 3. 2. 2. -1.26 -3.9 0.67 0.785 0. 0. 0.
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-0.0220583 1. 3. 2. 2. -1.23 -4.7 0.67 1.33 0. 0. 0.
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-1.63148 4. 3. 2. 2. -16.8 -413. 1.15 0.86 0. 0. 0.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-161 of Wu and Zhou (2012).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Wu, J. and Zhou, Y.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0 0.0
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2.059 420.0
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9.253 1548.0
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6.088 3882.0
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@EOS !---Equation of state---
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FE2 !Helmholtz equation of state for R-161 of Lemmon (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W.
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? preliminary equation, 2005.
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?
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?Uncertainties in density are less than 1% below 250 K, less than 2% below 300 K,
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? and up to 5% at higher temperatures. Uncertainties in vapor pressure are 1%
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? at temperatures down to 230 K, and 5% or higher at temperatures below 230 K.
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? Uncertainties in heat capacities and sound speeds in the liquid may be as
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? high as 15%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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130.0 !Lower temperature limit [K]
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400.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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20.0 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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48.0595 !Molar mass [g/mol]
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130.0 !Triple point temperature [K]
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0.005916 !Pressure at triple point [kPa]
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19.95 !Density at triple point [mol/L]
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235.6 !Normal boiling point temperature [K]
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0.222 !Acentric factor
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375.3 5091.0 6.28 !Tc [K], pc [kPa], rhoc [mol/L] (218.5 kg/m^3)
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375.3 6.28 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.75688 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-1.4110 1.25 1. 0.
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-0.63922 1.5 1. 0.
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0.055685 0.25 3. 0.
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0.00028395 0.875 7. 0.
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0.73357 2.375 1. 1.
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0.67596 2.0 2. 1.
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0.011369 2.125 5. 1.
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-0.56406 3.5 1. 2.
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-0.094362 6.5 1. 2.
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-0.16780 4.75 4. 2.
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0.00034215 12.5 2. 3.
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@AUX !---Auxiliary function for Cp0
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CP2 !Ideal gas heat capacity function for R-161 of Lemmon (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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3.985 0.0
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2.077 420.0
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9.265 1548.0
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6.054 3882.0
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@EOS !---Equation of state---
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ECS !Extended Corresponding States model w/ T-dependent shape factors, R125 reference, for R-161.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?predicted using ECS method, R125 reference
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?Huber, M.L. and Ely, J.F.,
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? "A predictive extended corresponding states model for pure and mixed
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? refrigerants including an equation of state for R134a,"
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? Int. J. Refrigeration, 17(1):18-31, 1994. doi: 10.1016/0140-7007(94)90083-3
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?
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?DATA SOURCES
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? References on fixed points:
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? Tc, Pc: experimental value, est. unc. <1% for Tc, <3% on Pc
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? Ambrose, D., "Vapor-Liquid Critical Properties," National Physical Laboratory Report Chem 107, Middlesex, United Kingdom (1980)
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? Rhoc: predicted by Fedors method, est. unc. < 25%
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? Tt: experimental value, estimated unc < 1%, Grosse, A.V., Wackher, R.C., Linn, C.B., "Physical Properties of the Alkyl Fluorides and a Comparison of the Alkyl Fluorides with the Other Alkyl Halides and with the Alkyls of the Elements of Period II," J. Phys. Chem., 44, 275 (1940) doi: 10.1007/s10765-004-7731-8
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?
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?Reference for saturated liquid density: Grosse, A.V., Wackher, R.C., Linn, C.B., "Physical Properties of the Alkyl Fluorides and a Comparison of the Alkyl Fluorides with the Other Alkyl Halides and with the Alkyls of the Elements of Period II," J. Phys. Chem., 44, 275 (1940)est. unc, <1% over 163-236 K.
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?Reference for vapor pressure: Vidaurri, F.C., "Ethyl Fluoride Vapor Pressure," J. Chem. Eng. Data, 20, 349 (1975) doi: 10.1021/je60067a005, est. unc. <3% over 169-375 K.
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?
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!```````````````````````````````````````````````````````````````````````````````
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129.95 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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30.0 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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R125.FLD
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BWR !Pointer to reference fluid model
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0.30349 !Acentric factor for R125 used in shape factor correlation
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0.27022 !Critical compressibility for R125 used in correlation
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0.21999 !Acentric factor for fluid used in shape factor correlation
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375.31 !Critical temperature [K]
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5028.0 !Critical pressure [kPa]
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6.1020259 !Critical density [mol/L]
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2 !Number of temperature coefficients for 'f' shape factor
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0.028907925 0. !Alpha1 of Huber & Ely
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-1.123811813 1. !Alpha2 (log(Tr) term)
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1 !Number of density coefficients for 'f' shape factor
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0.0078973712 1. !Rho coefficient and power in temperature
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2 !Number of temperature coefficients for 'h' shape factor
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-0.088432119 0. !Beta1 of Huber & Ely
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0.841031307 1. !Beta2 (log(Tr) term)
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1 !Number of density coefficients for 'h' shape factor
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-0.033341505 1. !Rho coefficient and power in temperature
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^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
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#ETA !---Viscosity---
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VS1 !Pure fluid viscosity model for R-161 of Tsolakidou et al. (2017).
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:DOI: 10.1063/1.4983027
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tsolakidou, Ch.M., Assael, M.J., Huber, M.L., and Perkins, R.A.,
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? "Reference Correlations of the Viscosity and Thermal Conductivity of Ethyl Fluoride (R161),"
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? J. Phys. Chem. Ref. Data, 46, 023103, 2017.
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? doi: 10.1063/1.4983027
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?
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!```````````````````````````````````````````````````````````````````````````````
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130.0 !Lower temperature limit [K]
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450.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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19.95 !Maximum density [mol/L]
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1 !Number of terms associated with dilute-gas function
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CI1 !Pointer to reduced effective collision cross-section model
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0.4457 !Lennard-Jones coefficient sigma [nm]
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320.39 !Lennard-Jones coefficient epsilon/kappa [K]
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1.0 1.0 !Reducing parameters for T, eta
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0.14805732 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
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9 !Number of terms for initial density dependence
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320.39 0.0533186 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
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-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
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219.73999 -0.25
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-1015.3226 -0.5
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2471.0125 -0.75
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-3375.1717 -1.0
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2491.6597 -1.25
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-787.26086 -1.5
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14.085455 -2.5
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-0.34664158 -5.5
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0 4 2 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
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375.25 6.2839 1.0 !Reducing parameters for T, rho, eta (correlation in terms of uPa-s)
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-10.28373 0.5 0.6666666667 0. 0 !Coefficient, power of tau, del
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7.65563 0.5 1.6666666667 0. 0
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4.842 2.5 0.6666666667 0. 0
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0.42223 0.5 4.6666666667 0. 0
|
||
64.34983 0.5 1.6666666667 0. 0
|
||
64.34983 1.5 0.6666666667 0. 0
|
||
10.99213 2.0 0.0 0. 0
|
||
-1.0 2.0 2.0 0. 0
|
||
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-161.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Tsolakidou et al., 2017.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
2 !Number of terms
|
||
0.2413 0 !Coefficient, power of Tstar
|
||
-0.45 1
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for R-161 of Tsolakidou et al. (2017).
|
||
:DOI: 10.1063/1.4983027
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Tsolakidou, Ch.M., Assael, M.J., Huber, M.L., and Perkins, R.A.,
|
||
? "Reference Correlations of the Viscosity and Thermal Conductivity of Ethyl Fluoride (R161),"
|
||
? J. Phys. Chem. Ref. Data, 46, 023103, 2017.
|
||
? doi: 10.1063/1.4983027
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
130.0 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
19.95 !Maximum density [mol/L]
|
||
6 5 !# terms for dilute gas function: numerator, denominator
|
||
375.25 0.001 !Reducing parameters for T, tcx
|
||
7.96804 0.
|
||
-12.5874 1.
|
||
-26.3743 2.
|
||
16.9894 3.
|
||
127.545 4.
|
||
-32.548 5.
|
||
5.406 0.
|
||
-18.8331 1.
|
||
24.868 2.
|
||
-9.14139 3.
|
||
1.0 4.
|
||
10 0 !# terms for background gas function: numerator, denominator
|
||
375.25 6.2839 0.001 !Reducing parameters for T, rho, tcx
|
||
-8.41553 0. 1. 0.
|
||
-39.7744 0. 2. 0.
|
||
106.179 0. 3. 0.
|
||
-53.2351 0. 4. 0.
|
||
8.23094 0. 5. 0.
|
||
7.41456 1. 1. 0.
|
||
44.0586 1. 2. 0.
|
||
-81.9833 1. 3. 0.
|
||
37.6052 1. 4. 0.
|
||
-4.90293 1. 5. 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-161 of Tsolakidou et al. (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Tsolakidou, Ch.M., Assael, M.J., Huber, M.L., and Perkins, R.A.,
|
||
? "Correlations for the Viscosity and Thermal Conductivity of Ethyl Fluoride (R161),"
|
||
? J. Phys. Chem. Ref. Data, 46, 023103, 2017.
|
||
? doi: 10.1063/1.4983027
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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)
|
||
0.065 !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)
|
||
0.183e-9 !Xi0 (amplitude) [m]
|
||
0.055 !Gam0 (amplitude) [-]
|
||
0.3104e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
562.88 !Tref (reference temperature) [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); fit to limited data for R-161.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Reference for vapor pressure: Vidaurri, F.C., "Ethyl Fluoride Vapor Pressure," J. Chem. Eng. Data, 20, 349 (1975) doi: 10.1021/je60067a005, est. unc. <3% over 169-375 K.
|
||
?Huber, M.L., Laesecke, A., and Perkins, R.A.
|
||
? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
|
||
? a New Correlation for the Viscosity of R134a,"
|
||
? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
|
||
?
|
||
?VISCOSITY
|
||
? Meng, X., Gu, X., Wu, J., Bi, S., Viscosity Measurements of Ethyl Fluoride (R161) from 243 K to 363 K at Pressures up to 30 MPa, Int. J. Thermophys., 2015, 36, 2497-2506 doi: 10.1007/s10765-013-1546-4 Estimated uncertainty 5 % in liquid to 350 K to 30 MPa and in atmospheric pressure gas
|
||
?
|
||
?THERMAL CONDUCTIVITY
|
||
? Yao, C., Zhao, X., Lv, S., Guo, Z., Thermal conductivity of ethyl fluoride (HFC161) Fluid Phase Equilib., 2014, 375, 228-235 doi: 10.1016/j.fluid.2014.04.038 Estimated uncertainty 5 % in saturated liquid to 350 K and in gas phase above 280 K. Data for comparison unavailable in compressed liquid
|
||
?
|
||
?The Lennard-Jones parameters were found from fitting experimental data of Lv et al. (2014)
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
130.0 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
19.95 !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)
|
||
0.4457 !Lennard-Jones coefficient sigma [nm]
|
||
320.39 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
||
3.78024e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
2.48902e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
3 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
0.997775 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0772641 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0227973 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
0.873783 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0273054 0. 1. 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-161 of Mulero et al. (2012).
|
||
:DOI: 10.1063/1.4768782
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A., Cachadi<64>a, 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
|
||
375.3 !Critical temperature used in fit (dummy)
|
||
0.05385 1.111 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-161 of Gao (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K., 2017.
|
||
?
|
||
?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. !
|
||
375.25 5046.0 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-7.5088 1.0
|
||
3.5250 1.5
|
||
-3.1586 2.0
|
||
-2.5577 4.8
|
||
-2.7114 15.8
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-161 of Gao (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K., 2017.
|
||
?
|
||
?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. !
|
||
375.25 6.2839 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
4.4371 0.5
|
||
-10.8 1.05
|
||
23.734 1.5
|
||
-17.962 1.9
|
||
3.601 3.1
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-161 of Gao (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K., 2017.
|
||
?
|
||
?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. !
|
||
375.25 6.2839 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-10.946 0.595
|
||
23.462 0.95
|
||
-32.327 1.3
|
||
9.68 1.75
|
||
-29.123 3.9
|
||
-78.606 9.2
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
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|