Isobutane !Short name 75-28-5 !CAS number 2-Methylpropane !Full name CH(CH3)3 !Chemical formula {C4H10} R-600a !Synonym 58.1222 !Molar mass [g/mol] 113.73 !Triple point temperature [K] 261.401 !Normal boiling point [K] 407.81 !Critical temperature [K] 3629.0 !Critical pressure [kPa] 3.879756788 !Critical density [mol/L] 0.184 !Acentric factor 0.132 !Dipole moment [Debye]; DIPPR: from Nelson, NBS, NSRDS 10 (1967). IIR !Default reference state 10.0 !Version number 1969 !UN Number :UN: br-alkane !Family :Family: 2868.20 !Heating value (upper) [kJ/mol] :Heat: 4000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C4H10/c1-4(2)3/h4H,1-3H3 !Standard InChI String :InChi: NNPPMTNAJDCUHE-UHFFFAOYSA-N !Standard InChI Key :InChiKey: 7b3b4080 (butane) !Alternative fluid for mixing rules :AltID: 47ade7e0 !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 ! 02-01-96 MM, Original version. ! 10-24-96 MM, Add thermal conductivity model of Younglove and Ely. ! 11-18-98 EWL, Add equation of state of Polt et al. (1992). ! 11-01-99 EWL, Add Span 12 term short equation of state. ! 07-17-00 EWL, Add Vogel viscosity equation. ! 03-29-01 MLH, Add new thermal conductivity correlation for ic4 (Perkins, 2001). ! 05-14-01 EWL, Add Miyamoto and Watanabe equation. ! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation. ! 09-02-04 EWL, Add Buecker and Wagner equation. ! 10-13-04 MLH, Add family. ! 08-08-05 EWL, Change Ptrp in melting line equation changed to match EOS at Ttrp. ! 12-02-06 MLH, Update LJ for ECS. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ! 12-30-13 EWL, Change upper limit to 200 MPa based on data of Miyamoto and Uematsu, J. Chem. Thermodyn., 2006, 38:360-366, with maximum deviation of 0.4% in density. See also the new high pressure and temperature data of Ito, Nagata, and Miyamoto, Int. J. Thermophys, 2013. ! 02-16-17 KG, Add ancillary equations. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for isobutane of Buecker and Wagner (2006). :TRUECRITICALPOINT: 407.81 3.879756788 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1063/1.1901687 ? ?``````````````````````````````````````````````````````````````````````````````` ?Bücker, D. and Wagner, W., ? "Reference Equations of State for the Thermodynamic Properties of Fluid ? Phase n-Butane and Isobutane," ? J. Phys. Chem. Ref. Data, 35(1):929-1019, 2006. doi: 10.1063/1.1901687 ? ?The uncertainties in density are 0.02% at temperatures below 340 K and ? pressures below 12 MPa (both liquid and vapor states), 0.3% at temperatures ? below 300 K and pressures above 12 MPa, 0.1% in the vapor phase between 340 and ? 450 K, and 0.5% elsewhere. In the critical region, deviations in pressure are ? 0.5%. Uncertainties in heat capacities are typically 1-2%, rising to 5% in the ? critical region and at temperatures below 200 K. Uncertainties in the speed of ? sound are typically 1-2%, rising to 5% at temperatures below 200 K and in the ? critical region. ? !``````````````````````````````````````````````````````````````````````````````` 113.73 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 12.9 !Maximum density [mol/L] CPP !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 113.73 !Triple point temperature [K] 0.00002289 !Pressure at triple point [kPa] 12.74 !Density at triple point [mol/L] 261.401 !Normal boiling point temperature [K] 0.184 !Acentric factor 407.81 3629.0 3.879756788 !Tc [K], pc [kPa], rhoc [mol/L] 407.81 3.879756788 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 23 4 2 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 2.0686820727966 0.5 1. 0. !a(i),t(i),d(i),l(i) -3.6400098615204 1.0 1. 0. 0.51968754427244 1.5 1. 0. 0.17745845870123 0.0 2. 0. -0.12361807851599 0.5 3. 0. 0.045145314010528 0.5 4. 0. 0.03047647996598 0.75 4. 0. 0.75508387706302 2.0 1. 1. -0.85885381015629 2.5 1. 1. 0.036324009830684 2.5 2. 1. -0.01954879945055 1.5 7. 1. -0.004445239290496 1.0 8. 1. 0.004641076366646 1.5 8. 1. -0.071444097992825 4.0 1. 2. -0.080765060030713 7.0 2. 2. 0.15560460945053 3.0 3. 2. 0.0020318752160332 7.0 3. 2. -0.10624883571689 3.0 4. 2. 0.039807690546305 1.0 5. 2. 0.016371431292386 6.0 5. 2. 0.00053212200682628 0.0 10. 2. -0.0078681561156387 6.0 2. 3. -0.0030981191888963 13.0 6. 3. -0.042276036810382 2.0 1. 2. 2. -10.0 -150.0 1.16 0.85 0. 0. 0. -0.0053001044558079 0.0 2. 2. 2. -10.0 -200.0 1.13 1.0 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 isobutane of Buecker and Wagner (2006). ? ?``````````````````````````````````````````````````````````````````````````````` ?Bücker, D. and Wagner, W., 2006. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.05956619 0.0 4.94641014 387.94064 4.09475197 973.80782 15.6632824 1772.71103 9.73918122 4228.52424 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for isobutane of Buecker and Wagner (2006). ? ?``````````````````````````````````````````````````````````````````````````````` ?Bücker, D. and Wagner, W., 2006. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 3.05956619 1.0 !ai, ti for [ai*log(tau**ti)] terms -5.9995196315283579 0.0 !aj, ti for [ai*tau**ti] terms 5.0189508361247883 1.0 !aj, ti for [ai*tau**ti] terms 4.94641014 387.94064 !aj, ti for [ai*log(1-exp(-ti/T)] terms 4.09475197 973.80782 15.6632824 1772.71103 9.73918122 4228.52424 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for isobutane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Bücker, D. and Wagner, W., 2006. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 3.05956619 1.0 !ai, ti for [ai*log(tau**ti)] terms 11.60865546 0.0 !aj, ti for [ai*tau**ti] terms -5.29450411 1.0 4.94641014 -0.9512779015 !aj, ti for [ai*log(1-exp(ti*tau)] terms 4.09475197 -2.3878958853 15.6632824 -4.3469042691 9.73918122 -10.3688586351 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FEK !Helmholtz equation of state for isobutane of Kunz and Wagner (2004). ? ?``````````````````````````````````````````````````````````````````````````````` ?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M. ? "The GERG-2004 Wide-Range Equation of State for Natural Gases ? and Other Mixtures," GERG Technical Monograph 15, ? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007. ? !``````````````````````````````````````````````````````````````````````````````` 113.73 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.9 !Maximum density [mol/L] PHK !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 113.73 !Triple point temperature [K] 0.00002177 !Pressure at triple point [kPa] 12.78 !Density at triple point [mol/L] 261.42 !Normal boiling point temperature [K] 0.1841 !Acentric factor 407.817 3633.1 3.86014294 !Tc [K], pc [kPa], rhoc [mol/L] 407.817 3.86014294 !Reducing parameters [K, mol/L] 8.314472 !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 1.0429331589100 0.25 1. 0. -2.8184272548892 1.125 1. 0. 0.8617623239785 1.5 1. 0. -0.10613619452487 1.375 2. 0. 0.098615749302134 0.25 3. 0. 0.00023948208682322 0.875 7. 0. 0.30330004856950 0.625 2. 1. -0.041598156135099 1.75 5. 1. -0.29991937470058 3.625 1. 2. -0.080369342764109 3.625 4. 2. -0.029761373251151 14.5 3. 3. 0.01305963030314 12.0 4. 3. @AUX !---Auxiliary function for PH0 PHK !Ideal gas Helmholtz form for isobutane of Kunz and Wagner (2004). ? ?``````````````````````````````````````````````````````````````````````````````` ?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 0 2 2 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 3.06714 1.0 !ai, ti for [ai*log(tau**ti)] terms 20.413726078 0.0 !aj, ti for [ai*tau**ti] terms -94.467620036 1.0 -5.25156 0.485556021 !aj, ti for cosh and sinh terms -16.1388 2.19158348 8.97575 1.074673199 25.1423 4.671261865 @EOS !---Equation of state--- FE1 !Helmholtz equation of state for isobutane of Miyamoto and Watanabe (2001). ? ?``````````````````````````````````````````````````````````````````````````````` ?Miyamoto, H. and Watanabe, K. ? "A Thermodynamic Property Model for Fluid-Phase Isobutane," ? Int. J. Thermophys., 23(2):477-499, 2002. ? ?The uncertainties of the equation of state are approximately 0.2% ? in density, 1% in heat capacity, 1% in the speed of sound, and ? 0.2% in vapor pressure, except in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 113.56 !Lower temperature limit [K] 573.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.90 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 113.56 !Triple point temperature [K] 0.000021 !Pressure at triple point [kPa] 12.738 !Density at triple point [mol/L] 261.48 !Normal boiling point temperature [K] 0.185 !Acentric factor 407.817 3640.0 3.8601429 !Tc [K], pc [kPa], rhoc [mol/L] 407.817 3.8601429 !Reducing parameters [K, mol/L] 8.314472 !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 0.2892737 -0.25 1. 0. !a(i),t(i),d(i),l(i) -1.342570 1.5 1. 0. -0.007976713 -0.75 2. 0. 0.2025793 0.0 2. 0. -0.04241612 1.25 3. 0. 0.002617971 1.5 5. 0. 5.068955e-5 0.5 8. 0. -1.144596e-6 2.5 8. 0. -1.930153 1.5 3. 1. 1.982609 1.75 3. 1. 0.002076533 -0.25 8. 1. -0.004958752 3.0 5. 1. 0.001377372 3.0 6. 1. -0.1582662 4.0 1. 2. -0.04961892 2.0 5. 2. 9.45103e-4 -1.0 7. 2. -0.03037276 2.0 2. 3. -0.01382675 19.0 3. 3. 8.876254e-5 5.0 15. 3. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for isobutane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Miyamoto, H. and Watanabe, K. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.059347 0.0 4.940314 387.75987 4.090139 972.01102 9.739581 4235.81166 15.68832 1772.81924 @EOS !---Equation of state--- BWR !MBWR equation of state for isobutane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., ? "Thermophysical properties of fluids. II. Methane, ethane, propane, ? isobutane and normal butane," ? J. Phys. Chem. Ref. Data, 16:577-798, 1987. ? ?The uncertainty in density is 0.1%. The uncertainty is ? 2% for heat capacities, 0.5% for the speed of sound in the vapor, and 1% ? for the speed of sound in the liquid. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.89 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 113.55 !Triple point temperature [K] 1.948e-5 !Pressure at triple point [kPa] 12.755 !Density at triple point [mol/L] 261.537 !Normal boiling point temperature [K] 0.18534 !Acentric factor 407.85 3640.0 3.860 !Tc [K], pc [kPa], rhoc [mol/L] 407.85 3.860 !Reducing parameters [K, mol/L] 3.860 !gamma 0.0831434 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term 0.01307325972 0.3927802742 -31.85427394 7608.825192 -1753919.859 -0.002090019755 8.959557971 -6816.71013 -1111271.045 0.0003248737572 -1.046526456 653.6598969 0.03726503734 8.553649395 2109.987236 -1.401267363 0.05213089327 -19.25026382 0.7640067895 3425854.273 -337347592.4 118068.3444 0.1529683738e+10 3323.837416 64231.69487 38.91706042 -1494755.736 -0.01720240173 289.4195375 0.002005086329 -0.4448393005 80.28488415 @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for isobutane of Younglove and Ely. ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31434 !Reducing parameters for T, Cp0 7 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 17027919.006 -3.0 -472697.24737 -2.0 4730.1406581 -1.0 -17.231723278 0.0 0.058491344291 1.0 8.9440351886e-6 2.0 -1.8274599197e-8 3.0 -19.283021962 3000.0 @EOS !---Equation of state--- FES !Helmholtz equation of state for isobutane of Span and Wagner (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Span, R. and Wagner, W. ? "Equations of State for Technical Applications. II. Results for Nonpolar Fluids," ? Int. J. Thermophys., 24(1):41-109, 2003. doi: 10.1023/A:1022310214958 ? ?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. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 12.89 !Maximum density [mol/L] CPS !Pointer to Cp0 model 58.123 !Molar mass [g/mol] 113.55 !Triple point temperature [K] 0.000020860 !Pressure at triple point [kPa] 12.784 !Density at triple point [mol/L] 261.42 !Normal boiling point temperature [K] 0.185 !Acentric factor 407.817 3640.0 3.8600898 !Tc [K], pc [kPa], rhoc [mol/L] 407.817 3.8600898 !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 1.0429332 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.8184273 1.125 1. 0. 0.86176232 1.5 1. 0. -0.10613619 1.375 2. 0. 0.098615749 0.25 3. 0. 0.00023948209 0.875 7. 0. 0.30330005 0.625 2. 1. -0.041598156 1.75 5. 1. -0.29991937 3.625 1. 2. -0.080369343 3.625 4. 2. -0.029761373 14.5 3. 3. 0.01305963 12.0 4. 3. @AUX !---Auxiliary function for Cp0 CPS !Ideal gas heat capacity function for isobutane of Jaeschke and Schley (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?Jaeschke, M. and Schley, P. ? "Ideal-Gas Thermodynamic Properties for Natural-Gas Applications," ? Int. J. Thermophys., 16(6):1381-1392, 1995. doi: 10.1007/BF02083547 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31451 !Reducing parameters for T, Cp0 1 0 2 2 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.06714 0.0 205919.6 -2.0 198.018 -1.0 -2.0 12891930.0 -2.0 893.765 -1.0 -2.0 1724067.0 -2.0 438.27 -1.0 -2.0 91243950.0 -2.0 1905.02 -1.0 -2.0 @EOS !---Equation of state--- FE3 !Helmholtz equation of state for isobutane of Polt et al. (1992). ? ?``````````````````````````````````````````````````````````````````````````````` ?Polt, A., Platzer, B., and Maurer, G., ? "Parameter der thermischen Zustandsgleichung von Bender fuer 14 ? mehratomige reine Stoffe," ? Chem. Tech. (Leipzig), 44(6):216-224, 1992. ? !``````````````````````````````````````````````````````````````````````````````` 120.0 !Lower temperature limit [K] 498.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.89 !Maximum density [mol/L] CP3 !Pointer to Cp0 model 58.124 !Molar mass [g/mol] 120.0 !Triple point temperature [K] 0.46491e-4 !Pressure at triple point [kPa] 12.649 !Density at triple point [mol/L] 261.51 !Normal boiling point temperature [K] 0.1851 !Acentric factor 407.85 3640.0 3.8607116 !Tc [K], pc [kPa], rhoc [mol/L] 407.85 3.8607116 !Reducing parameters [K, mol/L] 8.3143 !Gas constant [J/mol-K] 22 5 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -0.958589873652 3. 0. 0. 0. !a(i),t(i),d(i),l(i) 0.818846326211 4. 0. 0. 0. -0.115814967179 5. 0. 0. 0. 0.345513148715 0. 1. 0. 0. -1.68751721524 1. 1. 0. 0. 0.936693300209 2. 1. 0. 0. -1.06644545724 3. 1. 0. 0. 0.0980958295776 4. 1. 0. 0. 0.495941129005 0. 2. 0. 0. -0.261313404262 1. 2. 0. 0. 0.485109471188 2. 2. 0. 0. -0.177275820736 0. 3. 0. 0. -0.0209415485311 1. 3. 0. 0. 0.0788178884079 0. 4. 0. 0. -0.102751671767 1. 4. 0. 0. 0.0178645875838 1. 5. 0. 0. 0.958589873652 3. 0. 2. 1.0071072 -0.818846326211 4. 0. 2. 1.0071072 0.115814967179 5. 0. 2. 1.0071072 0.537585249054 3. 2. 2. 1.0071072 -0.719424468790 4. 2. 2. 1.0071072 0.245830118086 5. 2. 2. 1.0071072 @AUX !---Auxiliary function for Cp0 CP3 !Ideal gas heat capacity function for isobutane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Polt, A., Platzer, B., and Maurer, G., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 58.124 !Reducing parameters for T, Cp0 5 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 0.397893 0.0 0.00412501 1.0 -0.196195e-6 2.0 0.380185e-8 3.0 -0.52395e-11 4.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS1 !Pure fluid viscosity model for isobutane of Vogel et al. (2000). :DOI: 10.1023/A:1006623310780 ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Kuechenmeister, C., and Bich, E., ? "Viscosity Correlation for Isobutane over Wide Ranges of the Fluid Region," ? Int. J. Thermophys, 21(2):343-356, 2000. ? ?The uncertainty in viscosity varies from 0.4% in the dilute gas between ? room temperature and 600 K, to 3.0% over the rest of the fluid surface. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.90 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI1 !Pointer to reduced effective collision cross-section model 0.46445 !Lennard-Jones coefficient sigma [nm] 307.55 !Lennard-Jones coefficient epsilon/kappa [K] 1.0 1.0 !Reducing parameters for T, eta 0.1628213 0.5 !Chapman-Enskog term 9 !Number of terms for initial density dependence 307.55 0.0603345 !Reducing parameters for T (= eps/k), etaB2 (= 0.6022137*sigma**3) -19.572881 0.0 !Coefficient, power in T* = T/(eps/k) 219.73999 -0.25 -1015.3226 -0.5 2471.01251 -0.75 -3375.1717 -1.0 2491.6597 -1.25 -787.26086 -1.5 14.085455 -2.5 -0.34664158 -5.5 2 13 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 407.817 3.86 1.0 !Reducing parameters for T, rho, eta 2.33859774637 0.0 0. 0. 0 2.35255150838 0.5 0. 0. 0 103.511763411 0.0 2. 0. 0 -312.670896234 -1.0 2. 0. 0 145.253750239 -2.0 2. 0. 0 -210.649894193 0.0 3. 0. 0 386.269696509 -1.0 3. 0. 0 -214.963015527 -2.0 3. 0. 0 112.580360920 0.0 4. 0. 0 -223.242033154 -1.0 4. 0. 0 119.114788598 -2.0 4. 0. 0 -18.1909745900 0.0 5. 0. 0 36.0438957232 -1.0 5. 0. 0 -21.3960184050 -2.0 5. 0. 0 -1940.37606990 0.0 1. -1. 0 1940.37606990 0.0 1. 0. 0 1.0 0.0 0. 1. 0 -1.0 0.0 1. 0. 0 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) #AUX !---Auxiliary function for the collision integral CI1 !Collision integral model for isobutane of Vogel et al. (2000). ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Kuechenmeister, C., and Bich, E., 2000. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 3 !Number of terms 0.53583008 0 !Coefficient, power of Tstar -0.45629630 1 0.049911282 2 ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for isobutane of Perkins (2002). :DOI: 10.1021/je010121u ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., ? "Measurement and Correlation of the Thermal Conductivity of Isobutane ? from 114 K to 600 K at Pressures to 70 MPa," ? J. Chem. Eng. Data, 47(5):1272-1279, 2002. ? ?Uncertainty in thermal conductivity is 3%, except in the critical region ? and dilute gas which have an uncertainty of 5%. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 13.0 !Maximum density [mol/L] 3 0 !# terms for dilute gas function: numerator, denominator 407.85 1.0 !Reducing parameters for T, tcx -0.00237901 0. !Coefficient, power in T 0.0106601 1. 0.0215811 2. 10 0 !# terms for background gas function: numerator, denominator 407.85 3.86 1. !Reducing parameters for T, rho, tcx -0.0411789 0. 1. 0. !Coefficient, powers of T, rho, spare for future use 0.0476346 1. 1. 0. 0.146805 0. 2. 0. -0.128445 1. 2. 0. -0.11919 0. 3. 0. 0.107565 1. 3. 0. 0.0410226 0. 4. 0. -0.0385968 1. 4. 0. -0.00488704 0. 5. 0. 0.00520901 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 isobutane of Perkins (2002). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., ? "Measurement and Correlation of the Thermal Conductivity of Isobutane ? from 114 K to 600 K at Pressures to 70 MPa," ? J. Chem. Eng. Data, 47(5):1272-1279, 2002. ? !``````````````````````````````````````````````````````````````````````````````` 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) 1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1) 0.194e-9 !Xi0 (amplitude) [m] 0.0496 !Gam0 (amplitude) [-] 0.657661e-9 !Qd_inverse (modified effective cutoff parameter) [m] 611.73 !Tref (reference temperature) [K] ******************************************************************************** @TCX !---Thermal conductivity--- TC2 !Pure fluid thermal conductivity model for isobutane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., ? "Thermophysical properties of fluids. II. Methane, ethane, propane, ? isobutane and normal butane," ? J. Phys. Chem. Ref. Data, 16:577-798, 1987. ? ?The uncertainty in thermal conductivity is 2%, except in the critical region ? which is 10%. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 35000. !Upper pressure limit [kPa] 12.90 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.509217 !Lennard-Jones coefficient sigma [nm] 418.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.203525266 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 1.449797353 !Dilute gas terms (Eq 27): Gt(1) -0.1685643887 ! Gt(2) 0.004307008989 !Residual terms (Eqs 26, 28-30): Et(1) -1.509010974 469.3712392 -0.0003554280979 0.1841552874 -38.92338766 -0.09354624917 7.11433059 !Et(8) TK2 !Pointer to critical enhancement model (follows immediately) 0.0034718 !Critical enhancement terms (Eqs D1-D4): X1 10.1207 0.466392 1.00344 !X4 9.10218e-10 !Z 1.38054e-23 !Boltzmann's constant, k 1.6878386520 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) 0.0 !Fv(2) 1.40 !Fv(3) 407.85 !Fv(4) -20.55498053 !Coefficients for residual viscosity, eqs (22 - 25) 1357.076181 !Ev(2) (the viscosity is also used in conductivity correlation) 18.93774336 !Ev(3) -18222.77344 !Ev(4) -0.004599387773 !Ev(5) 63.05247065 !Ev(6) 12822.53921 !Ev(7) @ETA !---Viscosity--- VS2 !Pure fluid viscosity model for isobutane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., ? "Thermophysical properties of fluids. II. Methane, ethane, propane, ? isobutane and normal butane," ? J. Phys. Chem. Ref. Data, 16:577-798, 1987. ? ?The uncertainty in viscosity is 2%, except in the critical region which is 10%. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.90 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.509217 !Lennard-Jones coefficient sigma [nm] 418.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.203525266 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 0.5 !Exponent in Eq 19 for T 1.6878386520 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) 0.0 !Fv(2) 1.40 !Fv(3) 407.85 !Fv(4) -20.55498053 !Coefficients for residual viscosity, eqs (22 - 25) 1357.076181 !Ev(2) 18.93774336 !Ev(3) -18222.77344 !Ev(4) -0.004599387773 !Ev(5) 63.05247065 !Ev(6) 12822.53921 !Ev(7) 3.86 !Ev(8) NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) @AUX !---Auxiliary function for the collision integral CI2 !Collision integral model for isobutane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 !Number of terms -3.0328138281 0 !Omega (eq 20): coeffs of {(e/kT)**((4-n)/3)} 16.918880086 0 !There is misprint in Younglove and Ely, the exponent -37.189364917 0 ! is ((4-n)/3) not ((n+2)/3) 41.288861858 0 -24.61592114 0 8.948843096 0 -1.8739245042 0 0.209661014 0 !Wrong sign in Younglove and Ely, Table 2 -0.009657044 0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for isobutane. ? ?``````````````````````````````````````````````````````````````````````````````` ?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 ? ?Thermal conductivity and viscosity data used in the development of the ? extended corresponding states correlations were taken from: ? Younglove, B.A. and Ely, J.F., "Thermophysical properties of fluids. II. Methane, ethane, propane, isobutane and normal butane," J. Phys. Chem. Ref. Data, 16:577-798, 1987. ? ?The Lennard-Jones parameters were taken from Vogel, E., Kuechenmeister, C., and Bich, E., "Viscosity Correlation for Isobutane over Wide Ranges of the Fluid Region," Int. J. Thermophys, 21(2):343-356, 2000. ? !``````````````````````````````````````````````````````````````````````````````` 113.55 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 35000.0 !Upper pressure limit [kPa] 12.90 !Maximum density [mol/L] FEQ NITROGEN.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) 0.46445 !Lennard-Jones coefficient sigma [nm] 307.55 !Lennard-Jones coefficient epsilon/kappa [K] 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 1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.0 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 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 isobutane of Mulero et al. (2012). :DOI: 10.1063/1.4768782 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A., Cachadiña, 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. ! 2 !Number of terms in surface tension model 407.81 !Critical temperature used in fit (dummy) -0.01639 2.102 !Sigma0 and n 0.06121 1.304 #DE !---Dielectric constant--- DE3 !Dielectric constant model for isobutane of Harvey and Lemmon (2005). :DOI: 10.1007/s10765-005-2351-5 ? ?``````````````````````````````````````````````````````````````````````````````` ?Harvey, A.H. and Lemmon, E.W., ? "Method for Estimating the Dielectric Constant of Natural Gas Mixtures," ? Int. J. Thermophys., 26(1):31-46, 2005. doi: 10.1007/s10765-005-2351-5 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 273.16 1000.0 1.0 !Reducing parameters for T and D 1 2 4 0 0 0 !Number of terms in dielectric constant model 0.388417 -1. 1. 0. !Coefficient, T exp, D exp 20.534 0. 1. 0. 0.020 1. 1. 0. 126.25 0. 2. 0. 52.91 1. 2. 0. -7501.4 0. 2.9 0. -2672.9 1. 2.9 0. #MLT !---Melting line--- ML1 !Melting line model for isobutane of Buecker and Wagner (2005). :DOI: 10.1063/1.1901687 ? ?``````````````````````````````````````````````````````````````````````````````` ?Bücker, D. and Wagner, W., ? "Reference Equations of State for the Thermodynamic Properties of Fluid ? Phase n-Butane and Isobutane," ? J. Phys. Chem. Ref. Data, 35(1):929-1019, 2006. doi: 10.1063/1.1901687 ? !``````````````````````````````````````````````````````````````````````````````` 113.73 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 0. ! 0. ! 113.73 0.000022891 !Reducing temperature and pressure 2 0 0 0 0 0 !Number of terms in melting line equation -1953637129.0 0.0 !Coefficients and exponents 1953637130.0 6.12 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for isobutane 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. ! 407.81 3629.0 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -6.8729 1.0 1.6010 1.5 -0.94157 2.0 -2.9547 4.0 -2.0973 22.5 #DL !---Saturated liquid density--- DL2 !Saturated liquid density equation for isobutane of Buecker and Wagner (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?Functional Form: D=Dc*[1+SUM(Ni*Theta^(ti/3))] 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. ! 407.81 3.879756788 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 2.04025104 1.065 0.850874089 3.0 -0.479052281 4.0 0.348201252 7.0 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for isobutane 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. ! 407.81 3.879756788 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -1.9589 0.33 -5.9042 1.0 -17.630 3.0 -52.415 6.85 -127.72 16.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890