Butane !Short name 106-97-8 !CAS number n-Butane !Full name CH3-2(CH2)-CH3 !Chemical formula {C4H10} R-600 !Synonym 58.1222 !Molar mass [g/mol] 134.895 !Triple point temperature [K] 272.660 !Normal boiling point [K] 425.125 !Critical temperature [K] 3796.0 !Critical pressure [kPa] 3.922769613 !Critical density [mol/L] 0.201 !Acentric factor 0.05 !Dipole moment [Debye]; Harvey, A.H., Lemmon, E.W., Int. J. Thermophys., 26(1):31-46, 2005. IIR !Default reference state 10.0 !Version number 1011 !UN Number :UN: n-alkane !Family :Family: 2877.40 !Heating value (upper) [kJ/mol] :Heat: 4. !GWP (IPCC 2007) :GWP: 1000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C4H10/c1-3-4-2/h3-4H2,1-2H3 !Standard InChI String :InChi: IJDNQMDRQITEOD-UHFFFAOYSA-N !Standard InChI Key :InChiKey: 47ade7e0 (isobutane) !Alternative fluid for mixing rules :AltID: 7b3b4080 !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. ! 10-17-96 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. ! 03-30-01 MLH, Add Perkins et al. thermal conductivity equation (2001). ! 06-01-01 EWL, Add Miyamoto and Watanabe equation. ! 07-07-04 AHH, Update dipole moment. ! 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 slightly to match EOS at Ttrp. ! 12-02-06 MLH, Update LJ in ECS. ! 03-05-07 MLH, Add VS4 model. ! 09-13-10 EWL, Replace ancillary equations. ! 10-21-10 EWL, Increase upper pressure limit to 200 MPa based on data of Miyamoto (2008). ! 10-21-10 MLH, Revise upper limit of pressure on vis. and therm. cond. to 200 MPa. ! 04-11-12 MLH, Add extra blank FT coeff for consistent formatting. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ! 04-01-18 EWL, Add Herrmann and Vogel viscosity equation. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for butane of Buecker and Wagner (2006). :TRUECRITICALPOINT: 425.125 3.922769613 !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), 0.1% at temperatures ? below 270 K and pressures above 12 MPa, 0.2% between 340 and 515 K at ? pressures less than 0.6 MPa, and 0.4% elsewhere. Above the upper pressure ? limit of 69 MPa as given in the original formulation, new data up to 200 MPa ? show that the uncertainty in density is 0.3%. In the critical region, ? deviations in pressure are 0.5%. At temperatures above 500 K, the ? uncertainties in density increase up to 1%. Uncertainties in heat capacities ? are typically 1%, rising to 5% in the critical region and at pressures above ? 30 MPa. Uncertainties in the speed of sound are typically 0.5%, rising to 1% ? at temperatures below 200 K and to 4% in a large area around the critical point. ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] CPP !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 134.895 !Triple point temperature [K] 0.0006656 !Pressure at triple point [kPa] 12.645 !Density at triple point [mol/L] 272.660 !Normal boiling point temperature [K] 0.201 !Acentric factor 425.125 3796.0 3.922769613 !Tc [K], pc [kPa], rhoc [mol/L] 425.125 3.922769613 !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 2.5536998241635 0.5 1. 0. !a(i),t(i),d(i),l(i) -4.4585951806696 1.0 1. 0. 0.82425886369063 1.5 1. 0. 0.11215007011442 0.0 2. 0. -0.035910933680333 0.5 3. 0. 0.016790508518103 0.5 4. 0. 0.032734072508724 0.75 4. 0. 0.95571232982005 2.0 1. 1. -1.0003385753419 2.5 1. 1. 0.085581548803855 2.5 2. 1. -0.025147918369616 1.5 7. 1. -0.0015202958578918 1.0 8. 1. 0.004706068232642 1.5 8. 1. -0.097845414174006 4.0 1. 2. -0.04831790415876 7.0 2. 2. 0.17841271865468 3.0 3. 2. 0.018173836739334 7.0 3. 2. -0.11399068074953 3.0 4. 2. 0.019329896666669 1.0 5. 2. 0.001157587740101 6.0 5. 2. 0.00015253808698116 0.0 10. 2. -0.043688558458471 6.0 2. 3. -0.0082403190629989 13.0 6. 3. -0.028390056949441 2.0 1. 2. 2. -10.0 -150.0 1.16 0.85 0. 0. 0. 0.0014904666224681 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 butane 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 4.24680487 0.0 5.54913289 329.40404 11.4648996 1420.17366 7.59987584 2113.08938 9.66033239 4240.8573 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for butane 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)) 3.24680487 1.0 !ai, ti for [ai*log(tau**ti)] terms -5.4249697888268713 0.0 !aj, ti for [ai*tau**ti] terms 4.9194999371032626 1.0 !aj, ti for [ai*tau**ti] terms 5.54913289 329.40404 !aj, ti for [ai*log(1-exp(-ti/T)] terms 11.4648996 1420.17366 7.59987584 2113.08938 9.66033239 4240.8573 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for butane. ? ?``````````````````````````````````````````````````````````````````````````````` ?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 3.24680487 1.0 !ai, ti for [ai*log(tau**ti)] terms 12.54882924 0.0 !aj, ti for [ai*tau**ti] terms -5.46976878 1.0 5.54913289 -0.7748404445 !aj, ti for [ai*log(1-exp(ti*tau)] terms 11.4648996 -3.3406025522 7.59987584 -4.9705130961 9.66033239 -9.9755537783 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FEK !Helmholtz equation of state for butane of Kunz and Wagner (2007). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 69000.0 !Upper pressure limit [kPa] 13.2 !Maximum density [mol/L] PHK !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 134.895 !Triple point temperature [K] 0.0006507 !Pressure at triple point [kPa] 12.67 !Density at triple point [mol/L] 272.62 !Normal boiling point temperature [K] 0.2038 !Acentric factor 425.125 3830.3 3.920016792 !Tc [K], pc [kPa], rhoc [mol/L] 425.125 3.920016792 !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 1.0626277411455 0.25 1. 0. -2.8620951828350 1.125 1. 0. 0.88738233403777 1.5 1. 0. -0.12570581155345 1.375 2. 0. 0.10286308708106 0.250 3. 0. 0.00025358040602654 0.875 7. 0. 0.32325200233982 0.625 2. 1. -0.037950761057432 1.75 5. 1. -0.32534802014452 3.625 1. 2. -0.079050969051011 3.625 4. 2. -0.020636720547775 14.5 3. 3. 0.005705380933475 12.0 4. 3. @AUX !---Auxiliary function for PH0 PHK !Ideal gas Helmholtz form for butane of Kunz and Wagner (2007). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ? !``````````````````````````````````````````````````````````````````````````````` 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 3.33944 1.0 !ai, ti for [ai*log(tau**ti)] terms 20.884143364 0.0 !aj, ti for [ai*tau**ti] terms -91.638478026 1.0 -6.89406 0.43195766 !aj, ti for cosh and sinh terms -14.7824 2.124516319 9.44893 1.101487798 24.4618 4.502440459 @EOS !---Equation of state--- FE1 !Helmholtz equation of state for butane of Miyamoto and Watanabe (2001). ? ?``````````````````````````````````````````````````````````````````````````````` ?Miyamoto, H. and Watanabe, K. ? "A Thermodynamic Property Model for Fluid-Phase n-Butane," ? Int. J. Thermophys., 22(2):459-475, 2001. doi: 10.1023/A:1010722814682 ? ?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. ? !``````````````````````````````````````````````````````````````````````````````` 134.87 !Lower temperature limit [K] 589.0 !Upper temperature limit [K] 69000. !Upper pressure limit [kPa] 13.15 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 134.87 !Triple point temperature [K] 0.000688 !Pressure at triple point [kPa] 12.652 !Density at triple point [mol/L] 272.6 !Normal boiling point temperature [K] 0.2 !Acentric factor 425.125 3796.0 3.92001679 !Tc [K], pc [kPa], rhoc [mol/L] 425.125 3.92001679 !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 0.2952054 -0.25 1. 0. !a(i),t(i),d(i),l(i) -1.326360 1.50 1. 0. -0.002031317 -0.75 2. 0. 0.2240301 0.0 2. 0. -0.03635425 1.25 3. 0. 0.001905841 1.5 5. 0. 7.409154e-5 0.5 8. 0. -1.401175e-6 2.5 8. 0. -2.492172 1.50 3. 1. 2.386920 1.75 3. 1. 0.001424009 -0.25 8. 1. -0.009393388 3.0 5. 1. 0.00261659 3.0 6. 1. -0.1977323 4.0 1. 2. -0.03809534 2.0 5. 2. 0.001523948 -1.0 7. 2. -0.02391345 2.0 2. 3. -0.009535229 19.0 3. 3. 3.928384e-5 5.0 15. 3. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for butane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Miyamoto, H. and Watanabe, K., 2001. ? !``````````````````````````````````````````````````````````````````````````````` 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 4.240207 0.0 5.513671 327.55988 7.38845 1319.06935 10.25063 4138.63184 11.06101 1864.36783 @EOS !---Equation of state--- BWR !MBWR equation of state for butane 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 uncertainties in density are 0.05% in the liquid, 0.4% in the vapor ? and 0.06% in the supercritical and critical regions. The uncertainty is ? 2% for heat capacities, 1% for the speed of sound in the vapor, and 2% ? for the speed of sound in the liquid. All temperatures are given on IPTS-68. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 134.86 !Triple point temperature [K] 6.736e-4 !Pressure at triple point [kPa] 12.650 !Density at triple point [mol/L] 272.613 !Normal boiling point temperature [K] 0.199586 !Acentric factor 425.16 3796.0 3.920 !Tc [K], pc [kPa], rhoc [mol/L] 425.16 3.920 !Reducing parameters [K, mol/L] 3.920 !gamma 0.0831434 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term 0.0153740104603 -0.160980034611 -9.7978245901 499.660674504 -1021156.07687 0.00236032147756 -1.37475757093 -907.038733865 385421.748213 -0.3494537107e-4 0.157361122714 102.301474068 0.0182335737331 -4.04114307787 1.87979855783 0.36208879504 -0.00738762248266 -2.18618590563 0.118802729027 706854.198713 -219469885.796 -18245.4361268 0.206790377277e+10 111.757550145 55877.9925986 -15.9579054026 -1480342.14622 -0.245206328201 218.305259309 -0.923990627338e-4 -2.05267776639 38.763904482 @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for butane of Younglove and Ely. ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., 1987. ? !``````````````````````````````````````````````````````````````````````````````` 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 388023.10194 -3.0 -154442.9689 -2.0 2845.5082239 -1.0 -13.491511376 0.0 0.066142595353 1.0 -0.000024307965028 2.0 1.5044248429e-10 3.0 -8.3933423467 3000.0 @EOS !---Equation of state--- FES !Helmholtz equation of state for butane 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. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] CPS !Pointer to Cp0 model 58.123 !Molar mass [g/mol] 134.86 !Triple point temperature [K] 0.00064578 !Pressure at triple point [kPa] 12.671 !Density at triple point [mol/L] 272.62 !Normal boiling point temperature [K] 0.2 !Acentric factor 425.125 3796.0 3.9199628 !Tc [K], pc [kPa], rhoc [mol/L] 425.125 3.9199628 !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 1.0626277 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.8620952 1.125 1. 0. 0.88738233 1.5 1. 0. -0.12570581 1.375 2. 0. 0.10286309 0.25 3. 0. 0.00025358041 0.875 7. 0. 0.323252 0.625 2. 1. -0.037950761 1.75 5. 1. -0.32534802 3.625 1. 2. -0.079050969 3.625 4. 2. -0.020636721 14.5 3. 3. 0.0057053809 12.0 4. 3. @AUX !---Auxiliary function for Cp0 CPS !Ideal gas heat capacity function for butane 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 4.33944 0.0 232482.7 -2.0 183.636 -1.0 -2.0 12058640.0 -2.0 903.185 -1.0 -2.0 2071931.0 -2.0 468.27 -1.0 -2.0 89622620.0 -2.0 1914.1 -1.0 -2.0 @EOS !---Equation of state--- FE3 !Helmholtz equation of state for butane of Sarin et al. (2007). ? ?``````````````````````````````````````````````````````````````````````````````` ?Sarin, C., Astina, I.M., Darmanto, P.S., Sato, H. ? Thermodynamic property model of wide-fluid phase n-butane. ? Jurnal Teknik Mesin, 22(2):44-54, 2007. ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 589.0 !Upper temperature limit [K] 69000.0 !Upper pressure limit [kPa] 12.648 !Maximum density [mol/L] CPP !Pointer to Cp0 model 58.1222 !Molar mass [g/mol] 134.895 !Triple point temperature [K] 0.000677 !Pressure at triple point [kPa] 12.648 !Density at triple point [mol/L] 272.664 !Normal boiling point temperature [K] 0.201 !Acentric factor 425.125 3796.0 3.9200167922 !Tc [K], pc [kPa], rhoc [mol/L] 425.125 3.9200167922 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 18 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.7558424814 0.25 1. 0. 0.2874737492 0.25 2. 0. -0.0001142684008 0.5 8. 0. -1.811241776 1.25 1. 0. 0.01149143018 1.5 5. 0. -0.000004140496922 2.5 8. 0. 0.002458991872 3.5 2. 0. -0.005092499231 0.25 7. 1. 0.01042207957 0.5 8. 1. -0.03210318054 1. 7. 1. -3.055326240 1.5 3. 1. 2.730293235 1.75 3. 1. -0.01139148850 2. 7. 1. -0.04337857953 2. 5. 2. -0.1875707093 4. 1. 2. -0.006890261888 5. 7. 2. -0.009547267340 7. 2. 3. -0.01219583966 18. 3. 3. @EOS !---Equation of state--- FE4 !Helmholtz equation of state for butane 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. ? !``````````````````````````````````````````````````````````````````````````````` 140.0 !Lower temperature limit [K] 589.0 !Upper temperature limit [K] 30000.0 !Upper pressure limit [kPa] 12.81 !Maximum density [mol/L] CP4 !Pointer to Cp0 model 58.124 !Molar mass [g/mol] 140.0 !Triple point temperature [K] 0.00161 !Pressure at triple point [kPa] 12.573 !Density at triple point [mol/L] 272.62 !Normal boiling point temperature [K] 0.1984 !Acentric factor 425.14 3783.85 3.9192072 !Tc [K], pc [kPa], rhoc [mol/L] 425.14 3.9192072 !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 -0.504188295325 3. 0. 0. 0. !a(i),t(i),d(i),l(i) 0.541067401063 4. 0. 0. 0. -0.0760421383062 5. 0. 0. 0. 0.846035653528 0. 1. 0. 0. -1.91317317203 1. 1. 0. 0. 0.521441860186 2. 1. 0. 0. -0.783511318207 3. 1. 0. 0. 0.0689697797175 4. 1. 0. 0. 0.0947825461055 0. 2. 0. 0. -0.141401831669 1. 2. 0. 0. 0.382675021672 2. 2. 0. 0. -0.0423893176684 0. 3. 0. 0. 0.0677591792029 1. 3. 0. 0. 0.056794336334 0. 4. 0. 0. -0.131517698401 1. 4. 0. 0. 0.0221136942526 1. 5. 0. 0. 0.504188295325 3. 0. 2. 1.08974964 -0.541067401063 4. 0. 2. 1.08974964 0.0760421383062 5. 0. 2. 1.08974964 -0.061910953546 3. 2. 2. 1.08974964 0.423035373804 4. 2. 2. 1.08974964 -0.390505508895 5. 2. 2. 1.08974964 @AUX !---Auxiliary function for Cp0 CP4 !Ideal gas heat capacity function for butane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Polt, A., Platzer, B., and Maurer, G., 1992. ? !``````````````````````````````````````````````````````````````````````````````` 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 0.801601 0.0 0.000655936 1.0 0.000012277 2.0 -0.165626e-7 3.0 0.67736e-11 4.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS7 !Pure fluid viscosity model for butane of Herrman and Vogel (2018). :DOI: 10.1063/1.5020802 ? ?``````````````````````````````````````````````````````````````````````````````` ?Herrmann, S. and Vogel, E., ? "New Formulation for the Viscosity of n-Butane," ? J. Phys. Chem. Ref. Data, 47, 013104, 2018. ? doi: 10.1063/1.5020802 ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ! $VR RED TRED TEMP / =TR TR =TAU DENS DRED / =DEL ! !Dilute gas $DG CNST TR SQRT / SUMLOGT:3 EXP / ! !Initial density viscosity $VV CNST SUMTAU:9 DRED / * ! !Residual function $RF SUMTAUDEL:8 ! !Critical enhancement $CE 30 SIGN DEL 1 - SQR * 220 TAU 1 - ABS * - EXP SUMTAUDEL:1 * $CE 5 SIGN DEL 1 - SQR * 400 TAU 1 - ABS * - EXP SUMTAUDEL:1 * + ! !Coefficients $CF 1.0 425.125 3.922769613 0. 0 !Reducing parameters for eta, T, rho 1.0546549635209e3 0. 0. 0. 0 !Dilute gas terms 4.6147656002208 0. 0. 0. 0 4.5743185910390e-1 1. 0. 0. 0 3.0851104723224e-2 2. 0. 0. 0 4.89736312734e-1 0. 0. 0. 0 !Initial density terms -1.95728810000e1 0. 0. 0. 0 1.98887362343e2 0.25 0. 0. 0 -8.31764209120e2 0.50 0. 0. 0 1.83218450345e3 0.75 0. 0. 0 -2.26510439059e3 1. 0. 0. 0 1.51348864395e3 1.25 0. 0. 0 -4.32819866497e2 1.5 0. 0. 0 5.19698852489 2.5 0. 0. 0 -3.86579291550e-2 5.5 0. 0. 0 2.3460864383872 2. 2. 0. 0 !Residual function 7.8632175809804e-1 5. 2. 0. 0 1.5823593499816e1 0. 2.5 0. 0 -9.4670516989296 0. 3. 0. 0 1.0511496276340 0. 5. 0. 0 -1.9355799491084e-2 4. 7.5 0. 0 1.4895031937816e-4 5. 10. 0. 0 1.2280342363570e-3 2.5 10.733333333333333 0. 0 1.2790911462043 1. 1. 0. 0 2.5581822924086e-1 1. 1. 0. 0 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for butane of Perkins et al. (2002). :DOI: 10.1021/je0101202 ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A, Ramires, M.L.V., Nieto de Castro, C.A., and Cusco, L., ? "Measurement and Correlation of the Thermal Conductivity of Butane ? from 135 K to 600 K at Pressures to 70 MPa," ? J. Chem. Eng. Data, 47(5):1263-1271, 2002. doi: 10.1021/je0101202 ? ?Uncertainty in thermal conductivity is 3%, except in the critical region ? and dilute gas which have an uncertainty of 5%. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] 3 0 !# terms for dilute gas function: numerator, denominator 425.16 1.0 !Reducing parameters for T, tcx 0.00162676 0. !Coefficient, power in T 9.75703e-4 1. 0.0289887 2. 10 0 !# terms for background gas function: numerator, denominator 425.16 3.92 1. !Reducing parameters for T, rho, tcx -0.0304337 0. 1. 0. !Coefficient, powers of T, rho, spare for future use 0.0418357 1. 1. 0. 0.16582 0. 2. 0. -0.147163 1. 2. 0. -0.148144 0. 3. 0. 0.133542 1. 3. 0. 0.05255 0. 4. 0. -0.0485489 1. 4. 0. -0.00629367 0. 5. 0. 0.00644307 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 butane of Perkins et al. (2002). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., Ramires, M.L.V., Castro de Nieto, C.A., and Cusco, L., 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) [-] 0.87535e-9 !Qd_inverse (modified effective cutoff parameter) [m] 637.68 !Tref (reference temperature) [K] ******************************************************************************** @TCX !---Thermal conductivity--- TC2 !Pure fluid thermal conductivity model for butane 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%. All temperatures on IPTS-68 ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.503103 !Lennard-Jones coefficient sigma [nm] 440.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.203525266 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 1.530992335 !Dilute gas terms (Eq 27): Gt(1) -0.2114511021 ! Gt(2) 0.004024170074 !Residual terms (Eqs 26, 28-30): Et(1) 1.561435847 -600.4381127 -0.0007547260841 -0.02069676662 93.82534978 -0.1711371457 36.47724935 !Et(8) TK2 !Pointer to critical enhancement model (follows immediately) 0.000769608 !Critical enhancement terms (Eqs D1-D4): X1 13.2533 0.485554 1.01021 !X4 9.10218e-10 !Z 1.38054e-23 !Boltzmann's constant, k 1.630521851 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) 0.0 !Fv(2) 1.40 !Fv(3) 425.16 !Fv(4) -27.24386845 !Coefficients for residual viscosity, eqs (22 - 25) 801.2766611 !Ev(2) (the viscosity is also used in conductivity correlation) 25.03978646 !Ev(3) -13097.04275 !Ev(4) -0.08313305258 !Ev(5) 66.36975027 !Ev(6) 9849.317662 !Ev(7) @ETA !---Viscosity--- VS1 !Pure fluid viscosity model for butane of Vogel et al. (1999). ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Kuechenmeister, C., and Bich, E., ? "Viscosity for n-Butane in the Fluid Region," ? High Temp. - High Pressures, 31(2):173-186, 1999. ? ?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. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI1 !Pointer to reduced effective collision cross-section model 0.57335 !Lennard-Jones coefficient sigma [nm] 280.51 !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 280.51 0.1135034 !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 425.125 3.92 1.0 !Reducing parameters for T, rho, eta 2.30873963359 0.0 0. 0. 0 2.03404037254 0.5 0. 0. 0 -54.7737770846 0.0 2. 0. 0 58.0898623034 -1.0 2. 0. 0 0.0 -2.0 2. 0. 0 35.2658446259 0.0 3. 0. 0 -39.6682203832 -1.0 3. 0. 0 0.0 -2.0 3. 0. 0 -1.83729542151 0.0 4. 0. 0 0.0 -1.0 4. 0. 0 0.0 -2.0 4. 0. 0 -0.833262985358 0.0 5. 0. 0 1.93837020663 -1.0 5. 0. 0 0.0 -2.0 5. 0. 0 -188.075903903 0.0 1. -1. 0 188.075903903 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 butane of Vogel et al. (1999). ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Kuechenmeister, C., and Bich, E., 1999. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 3 !Number of terms 0.17067154 0 !Coefficient, power of Tstar -0.48879666 1 0.039038856 2 @ETA !---Viscosity--- VS2 !Pure fluid viscosity model for butane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Younglove, B.A. and Ely, J.F., 1987. ? ?The uncertainty in viscosity is 2%, except in the critical region which is 5%. ? All temperatures are given on IPTS-68. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.503103 !Lennard-Jones coefficient sigma [nm] 440.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.20352457 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 0.5 !Exponent in Eq 19 for T 1.630521851 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) 0.0 !Fv(2) 1.40 !Fv(3) 425.16 !Fv(4) -27.24386845 !Coefficients for residual viscosity, eqs (22 - 25) 801.2766611 !Ev(2) 25.03978646 !Ev(3) -13097.04275 !Ev(4) -0.08313305258 !Ev(5) 66.36975027 !Ev(6) 9849.317662 !Ev(7) 3.920 !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 butane 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 @ETA !---Viscosity--- VS4 !Pure fluid generalized friction theory viscosity model for butane of Quinones-Cisneros and Deiters (2006). ? ?``````````````````````````````````````````````````````````````````````````````` ?Quinones-Cisneros, S.E. and Deiters, U.K., ? "Generalization of the Friction Theory for Viscosity Modeling," ? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577 ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 68000.0 !Upper pressure limit [kPa] 13.86 !Maximum density [mol/L] 4 0 0 0 0 0 !Number of terms associated with dilute-gas function NUL !Pointer to reduced effective collision cross-section model; not used 0.503103 !Lennard-Jones coefficient sigma [nm] (not used) 440.0 !Lennard-Jones coefficient epsilon/kappa [K] (not used) 425.125 1.0 !Reducing parameters for T, eta 0.0 0.5 !Chapman-Enskog term; not used here 18.3983 0.0 !Empirical terms for eta0 -57.1255 0.25 49.3197 0.5 0 !Number of terms for initial density dependence -1.34110938674421e-5 -8.56587924603951e-5 -6.45720639242339e-13 0. 0. ! a(0),a(1),a(2) 1.49859653515567e-4 -1.71133855507542e-4 7.37953726544736e-13 0. 0. ! b(0),b(1),b(2) 3.53018109777015e-7 -1.93040375218067e-5 -1.26469933968355e-14 0. 0. ! c(0),c(1),c(2) -3.63389393526204e-9 -7.73717469888952e-10 0.0 0. 0. ! A(0),A(1),A(2) 3.70980259815724e-8 2.07658634467549e-9 0.0 0. 0. ! B(0),B(1),B(2) -1.12495594619911e-7 7.66906137372152e-8 0.0 0. 0. ! C(0),C(1),C(2) 0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2) 0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2) NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for butane. ? ?``````````````````````````````````````````````````````````````````````````````` ?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(4):577-798, 1987. doi: 10.1063/1.555785 ? ?The Lennard-Jones parameters were taken from Reid, R.C., Prausnitz, J.M., and Poling, B.E., "The Properties of Gases and Liquids," 4th edition, New York, McGraw-Hill Book Company, 1987. ? !``````````````````````````````````````````````````````````````````````````````` 134.86 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 13.86 !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) 0.57335 !Lennard-Jones coefficient sigma [nm] 280.51 !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 butane 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. ! 1 !Number of terms in surface tension model 425.125 !Critical temperature used in fit (dummy) 0.05138 1.209 !Sigma0 and n #DE !---Dielectric constant--- DE3 !Dielectric constant model for butane 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 0.0557549 -1. 1. 0. !Coefficient, T exp, D exp 20.611 0. 1. 0. 0.020 1. 1. 0. 66.64 0. 2. 0. 24.44 1. 2. 0. -7461.2 0. 3. 0. -1983.6 1. 3. 0. #MLT !---Melting line--- ML1 !Melting line model for butane 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 ? !``````````````````````````````````````````````````````````````````````````````` 134.895 !Lower temperature limit [K] 575.0 !Upper temperature limit [K] 0. ! 0. ! 134.895 0.00066566 !Reducing temperature and pressure 2 0 0 0 0 0 !Number of terms in melting line equation -558558235.4 0.0 !Coefficients and exponents 558558236.4 2.206 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for butane of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W., 2010. ? ?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc ? are the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 425.125 3796.0 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -7.1897 1.0 2.6122 1.5 -2.1729 2.0 -2.7230 4.5 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for butane of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W., 2010. ? ?Functional Form: D=Dc*[1+SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are ? the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 425.125 3.922769613 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 5.2341 0.44 -6.2011 0.60 3.6063 0.76 0.22137 5.0 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for butane of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W., 2010. ? ?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are ? the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 425.125 3.922769613 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -2.7390 0.391 -5.7347 1.14 -16.408 3.0 -46.986 6.5 -100.90 14.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890 @PS !Vapor pressure equation PS5 vapor pressure equation of Buecker and Wagner (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 425.125 3796.0 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -7.17616903 1.0 2.53635336 1.5 -2.07532869 2.0 -2.82241113 4.5 @DL !Saturated liquid density equation DL1 saturated liquid density equation of Buecker and Wagner (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 425.125 3.922769613 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 1.97874515 0.345 0.856799510 1.0 -0.341871887 1.5 0.304337558 3.0 @DV !Saturated vapor density equation DV6 saturated vapor density equation of Buecker and Wagner (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?Functional Form: D=Dc*EXP[SUM(Ni*Theta^(ti/3))*Tc/T] 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. ! 425.125 3.922769613 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -2.07770057 1.035 -3.08362490 2.5 -0.485645266 9.5 -3.83167519 12.5