Methane !Short name 74-82-8 !CAS number Methane !Full name CH4 !Chemical formula {CH4} R-50 !Synonym 16.0428 !Molar mass [g/mol] 90.6941 !Triple point temperature [K] 111.667 !Normal boiling point [K] 190.564 !Critical temperature [K] 4599.2 !Critical pressure [kPa] 10.139 !Critical density [mol/L] 0.01142 !Acentric factor 0.0 !Dipole moment [Debye]; (exactly zero due to symmetry) NBP !Default reference state 10.0 !Version number 1971, 1972 !UN Number :UN: n-alkane !Family :Family: 890.58 !Heating value (upper) at 25 C [kJ/mol] (ISO 6976:2016) :Heat: 25. !GWP (IPCC 2007) :GWP: A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/CH4/h1H4 !Standard InChI String :InChi: VNWKTOKETHGBQD-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 8ae7a700 !Hash number from InChI Key :Hash: !The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the ! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended ! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to ! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary ! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and ! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the ! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the ! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations, ! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and ! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface ! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a ! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The ! end of the fluid file is marked with @END. Anything below that is ignored. ! compiled by E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado ! 01-22-97 EWL, Original version. ! 06-24-98 EWL, Add Younglove and Ely BWR equation of state. ! 11-18-98 EWL, Add equation of state of Friend et al. (1989). ! 11-01-99 EWL, Add Span 12 term short equation of state. ! 01-26-00 EWL, Add Friend transport equations, but keep Younglove viscosity eq. as default since Friend eq. has an anomaly above 100 MPa. ! 07-23-02 EWL, Add sublimation line. ! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation. ! 10-13-04 MLH, Add family. ! 07-14-05 MLH, Add Vogel(2000) viscosity correlation. ! 12-02-06 MLH, Update LJ for ECS. ! 01-05-07 MLH, Add VS4 model, new VS1 model of Vogel, moved Friend VS1 model to EOF. ! 03-05-07 EWL, Add ancillary equations. ! 03-09-07 MLH, Add final FT model coefficients. ! 02-14-08 MLH, Add TK6 block for ECS for mixture calculations. ! 09-02-10 MLH, Add new VS4 model for viscosity feb2010 model. ! 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). ! 05-15-17 EWL, Change the hard coded CH4 model to the TK7 reverse Polish notation. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for methane of Setzmann and Wagner (1991). :TRUECRITICALPOINT: 190.564 10.139128 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1063/1.555898 ? ?``````````````````````````````````````````````````````````````````````````````` ?Setzmann, U. and Wagner, W., ? "A New Equation of State and Tables of Thermodynamic Properties for Methane ? Covering the Range from the Melting Line to 625 K at Pressures up to 1000 MPa," ? J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991. ? ?The uncertainties in density are 0.03% for pressures below 12 MPa and ? temperatures below 350 K and up to 0.07% for pressures less than 50 MPa. ? For the speed of sound, the uncertainty ranges from 0.03% (in the vapor ? phase) to 0.3% depending on temperature and pressure. Heat capacities ? may be generally calculated within an uncertainty of 1%. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] CPP !Pointer to Cp0 model 16.0428 !Molar mass [g/mol] 90.6941 !Triple point temperature [K] 11.696 !Pressure at triple point [kPa] 28.142 !Density at triple point [mol/L] 111.667 !Normal boiling point temperature [K] 0.01142 !Acentric factor 190.564 4599.2 10.139128 !Tc [K], pc [kPa], rhoc [mol/L] 190.564 10.139128 !Reducing parameters [K, mol/L] 8.31451 !Gas constant [J/mol-K] 36 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.04367901028 -0.5 1. 0. !a(i),t(i),d(i),l(i) 0.6709236199 0.5 1. 0. -1.765577859 1.0 1. 0. 0.8582330241 0.5 2. 0. -1.206513052 1.0 2. 0. 0.512046722 1.5 2. 0. -0.0004000010791 4.5 2. 0. -0.01247842423 0.0 3. 0. 0.03100269701 1.0 4. 0. 0.001754748522 3.0 4. 0. -0.3171921605e-5 1.0 8. 0. -0.224034684e-5 3.0 9. 0. 0.2947056156e-6 3.0 10. 0. 0.1830487909 0.0 1. 1. 0.1511883679 1.0 1. 1. -0.4289363877 2.0 1. 1. 0.06894002446 0.0 2. 1. -0.01408313996 0.0 4. 1. -0.0306305483 2.0 5. 1. -0.02969906708 2.0 6. 1. -0.01932040831 5.0 1. 2. -0.1105739959 5.0 2. 2. 0.09952548995 5.0 3. 2. 0.008548437825 2.0 4. 2. -0.06150555662 4.0 4. 2. -0.04291792423 12.0 3. 3. -0.0181320729 8.0 5. 3. 0.0344590476 10.0 5. 3. -0.00238591945 10.0 8. 3. -0.01159094939 10.0 2. 4. 0.06641693602 14.0 3. 4. -0.0237154959 12.0 4. 4. -0.03961624905 18.0 4. 4. -0.01387292044 22.0 4. 4. 0.03389489599 18.0 5. 4. -0.002927378753 14.0 6. 4. 0.9324799946e-4 2.0 2. 2. 2. -20.0 -200.0 1.07 1.0 0. 0. 0. -6.287171518 0.0 0. 2. 2. -40.0 -250.0 1.11 1.0 0. 0. 0. 12.71069467 1.0 0. 2. 2. -40.0 -250.0 1.11 1.0 0. 0. 0. -6.423953466 2.0 0. 2. 2. -40.0 -250.0 1.11 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 methane of Setzmann and Wagner (1991). ? ?``````````````````````````````````````````````````````````````````````````````` ?Setzmann, U. and Wagner, W., 1991. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31451 !Reducing parameters for T, Cp0 1 5 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0016 0.0 0.008449 648.0 4.6942 1957.0 3.4865 3895.0 1.6572 5705.0 1.4115 15080.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for methane of Setzmann and Wagner (1991). ? ?``````````````````````````````````````````````````````````````````````````````` ?Setzmann, U. and Wagner, W., 1991. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 5 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 3.0016 1.0 !ai, ti for [ai*log(tau**ti)] terms -2.9705496667947529 0.0 !aj, ti for [ai*tau**ti] terms 2.8907453831087553 1.0 !aj, ti for [ai*tau**ti] terms 0.008449 648.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 4.6942 1957.0 3.4865 3895.0 1.6572 5705.0 1.4115 15080.0 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for methane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Setzmann, U. and Wagner, W., 1991. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 5 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 3.0016 1.0 !ai, ti for [ai*log(tau**ti)] terms -2.9705496668 0.0 !aj, ti for [ai*tau**ti] terms 2.8907453831 1.0 0.008449 -3.4004324007 !aj, ti for [ai*log(1-exp(ti*tau)] terms 4.6942 -10.2695157532 3.4865 -20.43932747 1.6572 -29.9374488361 1.4115 -79.1335194475 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FEK !Helmholtz equation of state for methane 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. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] PHK !Pointer to Cp0 model 16.04246 !Molar mass [g/mol] 90.6941 !Triple point temperature [K] 11.698 !Pressure at triple point [kPa] 28.146 !Density at triple point [mol/L] 111.66 !Normal boiling point temperature [K] 0.0114 !Acentric factor 190.564 4599.2 10.139342719 !Tc [K], pc [kPa], rhoc [mol/L] 190.564 10.139342719 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 24 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.57335704239162 0.125 1. 0. -1.6760687523730 1.125 1. 0. 0.23405291834916 0.375 2. 0. -0.21947376343441 1.125 2. 0. 0.016369201404128 0.625 4. 0. 0.01500440638928 1.5 4. 0. 0.098990489492918 0.625 1. 1. 0.58382770929055 2.625 1. 1. -0.74786867560390 2.75 1. 1. 0.30033302857974 2.125 2. 1. 0.20985543806568 2.0 3. 1. -0.018590151133061 1.75 6. 1. -0.15782558339049 4.50 2. 2. 0.12716735220791 4.75 3. 2. -0.032019743894346 5.0 3. 2. -0.068049729364536 4.0 4. 2. 0.024291412853736 4.5 4. 2. 0.0051440451639444 7.5 2. 3. -0.019084949733532 14.0 3. 3. 0.0055229677241291 11.5 4. 3. -0.0044197392976085 26.0 5. 6. 0.040061416708429 28.0 6. 6. -0.033752085907575 30.0 6. 6. -0.0025127658213357 16.0 7. 6. @AUX !---Auxiliary function for PH0 PHK !Ideal gas Helmholtz form for methane 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 3.00088 1.0 !ai, ti for [ai*log(tau**ti)] terms 19.597508817 0.0 !aj, ti for [ai*tau**ti] terms -83.959667892 1.0 -0.0046 0.936220902 !aj, ti for cosh and sinh terms 4.46921 5.722644361 0.76315 4.306474465 8.74432 5.577233895 @EOS !---Equation of state--- FE1 !Helmholtz equation of state for methane of Friend et al. (1989). ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., ? "Thermophysical Properties of Methane," ? J. Phys. Chem. Ref. Data, 18(2):583-638, 1989. ? !``````````````````````````````````````````````````````````````````````````````` 90.6854 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 29.714 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 16.043 !Molar mass [g/mol] 90.6854 !Triple point temperature [K] 11.694 !Pressure at triple point [kPa] 28.145 !Density at triple point [mol/L] 111.66 !Normal boiling point temperature [K] 0.0086 !Acentric factor 190.551 4599.2 10.139 !Tc [K], pc [kPa], rhoc [mol/L] 190.551 10.139 !Reducing parameters [K, mol/L] 8.31451 !Gas constant [J/mol-K] 32 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.384436099659 0.0 1. 0. !a(i),t(i),d(i),l(i) -1.796925988 1.5 1. 0. 0.329444947369 2.5 1. 0. 0.0226312728442 -0.5 2. 0. 0.0759236768798 1.5 2. 0. 0.0693758447259 2.0 2. 0. 0.0241163263947 0.0 3. 0. 0.0107009920854 1.0 3. 0. -0.0380933275164 2.5 3. 0. 0.000471537561143 0.0 6. 0. 0.000556607678805 2.0 7. 0. 0.548759346533e-6 5.0 7. 0. -0.999632699967e-4 2.0 8. 0. -0.128087979280 5.0 1. 2. 0.0380198873377 6.0 1. 2. 0.139226650551 3.5 2. 2. -0.0874996348859 5.5 2. 2. -0.0033489416576 3.0 3. 2. -0.0517576297122 7.0 3. 2. 0.0252835179116 6.0 5. 2. 0.00051870320595 8.5 6. 2. -0.00166770594525 4.0 7. 2. -0.000607401927389 6.5 8. 2. -0.972915359991e-4 5.5 10. 2. -0.298844010462e-4 22.0 2. 4. -0.0130940111124 11.0 3. 4. 0.0198175833798 18.0 3. 4. 0.0208465762327 11.0 4. 4. -0.0358025052631 23.0 4. 4. -0.203486851741 17.0 5. 4. 0.215964755088 18.0 5. 4. -0.00429340628249 23.0 5. 4. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for methane. ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31451 !Reducing parameters for T, Cp0 4 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.5998324 0.0 0.2614717613495 0.3333333333333 -0.05671028952515 0.6666666666667 0.004105505612671 1.0 4.7206715 2009.15202 @EOS !---Equation of state--- FES !Helmholtz equation of state for methane 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. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] CPP !Pointer to Cp0 model 16.043 !Molar mass [g/mol] 90.6941 !Triple point temperature [K] 11.661 !Pressure at triple point [kPa] 28.167 !Density at triple point [mol/L] 111.66 !Normal boiling point temperature [K] 0.011 !Acentric factor 190.564 4599.0 10.139001 !Tc [K], pc [kPa], rhoc [mol/L] 190.564 10.139001 !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 0.89269676 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.5438282 1.125 1. 0. 0.64980978 1.5 1. 0. 0.020793471 1.375 2. 0. 0.070189104 0.25 3. 0. 0.00023700378 0.875 7. 0. 0.16653334 0.625 2. 1. -0.043855669 1.75 5. 1. -0.1572678 3.625 1. 2. -0.035311675 3.625 4. 2. -0.029570024 14.5 3. 3. 0.014019842 12.0 4. 3. @EOS !---Equation of state--- BWR !MBWR equation of state for methane 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. ? All temperatures on IPTS-68 ? !``````````````````````````````````````````````````````````````````````````````` 90.68 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 200000.0 !Upper pressure limit [kPa] 36.2029 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 16.043 !Molar mass [g/mol] 90.68 !Triple point temperature [K] 11.744 !Pressure at triple point [kPa] 28.147 !Density at triple point [mol/L] 111.667 !Normal boiling point temperature [K] 0.011 !Acentric factor 190.53 4597.97 10.15 !Tc [K], pc [kPa], rhoc [mol/L] 190.53 10.15 !Reducing parameters [K, mol/L] 10.15 !gamma 0.0831434 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term 0.9898937956e-4 0.2199608275 -5.322788 202.1657962 -22343.98926 0.000106794028 0.001457922469 -9.265816666 2915.364732 0.2313546209e-5 0.001387214274 0.04780467451 0.0001176103833 -0.00198209673 -0.2512887756 0.9748899826e-4 -0.1202192137e-5 0.0004128353939 -0.7215842918e-5 5081.738255 -919890.3192 -27.32264677 749902.4351 0.01114060908 10.83955159 -0.0004490960312 -13.80337847 -0.2371902232e-6 0.0003761652197 -0.2375166954e-8 -0.123764079e-6 0.6766926453e-5 @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for methane 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 -1804475.0507 -3.0 77426.666393 -2.0 -1324.1658754 -1.0 15.438149595 0.0 -0.051479005257 1.0 0.00010809172196 2.0 -0.65501783437e-7 3.0 -6.7490056171 3000.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS4 !Pure fluid generalized friction theory viscosity model for methane of Quinones-Cisneros et al. (2011). unpublished :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?Quinones-Cisneros, S.E., Huber, M.L., and Deiters, U.K., ? unpublished work, 2011. ? ?Detailed uncertainty analysis will be found in a future publication; however ? in general the estimated uncertainty in viscosity varies from less than 0.3% ? between 200-400 K for pressures less than 30 MPa, to less than 2% over the ? rest of the fluid surface up to 100 MPa, increasing up to 5% ? for 100 to 500 MPa, and 10% at 500 to 1000 MPa for temperatures to 625 K. ? Above uncertainties are valid when used with the equation of state of ? Setzmann, U. and Wagner, W., J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991. ? The use of other equations of state may result in larger uncertainties. ? !``````````````````````````````````````````````````````````````````````````````` 90.68 !Lower temperature limit [K] 1200.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] 6 0 0 0 0 0 !Number of terms associated with dilute-gas function NUL !Pointer to reduced effective collision cross-section model; not used 0.36652 !Lennard-Jones coefficient sigma [nm];not used 174.0 !Lennard-Jones coefficient epsilon/kappa [K];not used 190.564 1.0 !Reducing parameters for T, eta 0.0 0.5 !Chapman-Enskog term; not used here 58.343920516258155 0.0 -199.92388279110893 0.25 240.35409195445984 0.5 -113.08166560748158 0.75 21.645948012444557 1.0 0 !Number of terms for initial density dependence -0.00002946520026265898 0.000011850361299482738 0.0 0.0 0.0 ! a(0),a(1),a(2) 0.00002700022529490106 -0.000032677520832951284 0.0 0.0 0.0 ! b(0),b(1),b(2) 0.00002904479739920783 -0.00001018049342159992 -3.095500930526404e-8 0.0 0.0 ! c(0),c(1),c(2) 1.55372118714633e-8 -1.944037783173382e-9 0.0 0.0 0.0 ! A(0),A(1),A(2) -2.6710447337075816e-9 3.2621373142076857e-9 0.0 0.0 0.0 ! B(0),B(1),B(2) 5.207541202169661e-9 1.5949945307134116e-7 3.687831977089463e-10 0.0 0.0 ! C(0),C(1),C(2) 3.0218122078964884e-12 0.0 0.0 0.0 0.0 ! D(0),D(1),D(2) 0.0 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) ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for methane of Friend et al. (1989). :DOI: :WEB: https://nvlpubs.nist.gov/nistpubs/Legacy/TN/nbstechnicalnote1325.pdf ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., ? "Tables for the Thermophysical Properties of Methane," ? NIST Technical Note 1325, 1989. ? ?The uncertainty in thermal conductivity of the dilute gas between 130 ? and 625 K is 2.5%. For temperatures below 130 K, the uncertainty is ? less than 10%. Excluding the dilute gas, the uncertainty is 2% between ? 110 and 725 K at pressures up to 70 MPa, except near the critical ? point which has an uncertainty of 5% or greater. For the vapor at lower ? temperatures and the dense liquid near the triple point, an uncertainty of ? 10% is possible. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] 3 0 !# terms for dilute gas function: numerator, denominator 174.0 0.001 !Reducing parameters for T, tcx 1.45885 0. !Coefficient, power in T -0.4377162 -1. 0. -96. !Coefficient, power in T 8 0 !# terms for background gas function: numerator, denominator 190.551 10.139 0.00629638 !Reducing parameters for T, rho, tcx 1.5554612 0. 2. 0. !Coefficient, powers of T, rho, exp(rho) 1.0 0. 0. -99. !The order here is important 2.4149207 0. 1. 0. 0.55166331 0. 3. 0. -0.52837734 0. 4. 0. 0.073809553 -1. 4. 0. 0.24465507 0. 5. 0. -0.047613626 -1. 5. 0. TK7 !Pointer to critical enhancement auxiliary function #AUX !---Auxiliary function for the thermal conductivity critical enhancement TK7 !Thermal conductivity critical enhancement for methane of Friend et al. (1989). ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., 1989. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! $CE RED 1 TR - =TAU 1 DR - =DEL $CE 1 DPDT RGAS / DENS / CNST DENS POP< =V1 $CE CNST CNST DENS * DRED / TRED * DPDD / RGAS * DUP 0 POP> =V2 $CE CNST ETA / TRED TEMP / SQR / V1 SQR * V2 CNST POWR * $CE TAU ABS SQRT CNST * CNST DEL SQR * + CNST DEL * - SIGN EXP * $CF 0.001 190.564 10.139128 0. 0 1.E-12 0. 0. 0. 0 1.e5 0. 0. 0. 0 0.28631 0. 0. 0. 0 91.855 0. 0. 0. 0 0.4681 0. 0. 0. 0 2.646 0. 0. 0. 0 2.678 0. 0. 0. 0 0.637 0. 0. 0. 0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for methane. ? ?``````````````````````````````````````````````````````````````````````````````` ?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 ? ?The Lennard-Jones parameters were taken from Friend, D.G., Ely, J.F., and Ingham, H., "Tables for the Thermophysical Properties of Methane," NIST Technical Note 1325, 1989. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !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) 0.36652 !Lennard-Jones coefficient sigma [nm] 174.0 !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 ******************************************************************************** @TCX !---Thermal conductivity--- TC2 !Pure fluid thermal conductivity model for methane 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 5% in the liquid, 4% in the vapor, ? 3% at T>Tc, and 8% in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.368 !Lennard-Jones coefficient sigma [nm] 168.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.1069188 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 1.346953698 !Dilute gas terms (Eq 27): Gt(1) -0.3254677753 ! Gt(2) 0.002325800819 !Residual terms (Eqs 26, 28-30): Et(1) -0.2477927999 38.80593713 -0.1579519146e-6 0.003717991328 -0.9616989434 -0.03017352774 0.4298153386 !Et(8) TK2 !Pointer to critical enhancement model (follows immediately) 37.42368 !Critical enhancement terms (Eqs D1-D4): X1 3.16714 0.78035 0.60103 !X4 6.512707e-10 !Z 1.38054e-23 !Boltzmann's constant, k 0.16969859271 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) -0.013337234608 !Fv(2) 1.4 !Fv(3) 168. !Fv(4) -16.20427429 !Coefficients for residual viscosity, eqs (22 - 25) 427.0589027 !Ev(2) (the viscosity is also used in conductivity correlation) 14.02596278 !Ev(3) -3916.837745 !Ev(4) -0.0347709909 !Ev(5) 21.36542674 !Ev(6) 1436.802482 !Ev(7) @AUX !---Auxiliary function for the thermal conductivity critical enhancement TK3 !Simplified thermal conductivity critical enhancement for methane of Olchowy and Sengers (1989). ? ?``````````````````````````````````````````````````````````````````````````````` ?Olchowy, G.A. and Sengers, J.V., ? "A simplified representation for the thermal conductivity of fluids in the critical region," ? Int. J. Thermophysics, 10:417-426, 1989. doi: 10.1007/BF01133538 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 0 0 0 !# terms: CO2-terms, spare, spare, spare 1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)] 0.63 !Nu (universal exponent) 1.239 !Gamma (universal exponent) 1.03 !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) [-] 0.4e-9 !Qd_inverse (modified effective cutoff parameter) [m]; estmated value from matching Friend at 50 bar 285.846 !Tref (reference temperature)=1.5*Tc [K] @ETA !---Viscosity--- VS1 !Pure fluid viscosity model for methane of Vogel et al. (2000). ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Wilhelm, J., Kuechenmeister, C., and Jaesche, M., ? "High-precision viscosity measurements on methane," ? High Temp. - High Pressures, 32(1):73-81, 2000. ? ?The uncertainty in viscosity varies from 0.3% in the dilute gas between ? 260-360 K, to 3.0% over the rest of the fluid surface, increasing up to 5 % ? from 620 K and 100 MPa. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI1 !Pointer to reduced effective collision cross-section model 0.37333 !Lennard-Jones coefficient sigma [nm] 160.78 !Lennard-Jones coefficient epsilon/kappa [K] 1.0 1.0 !Reducing parameters for T, eta 0.0855422 0.5 !Chapman-Enskog term sqrt[MW]*0.021357 9 !Number of terms for initial density dependence 159.7 0.0306525 !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 1 9 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 190.564 10.139 1.0 !Reducing parameters for T, rho, eta 3.10860501398 0. 0. 0. 0 -3.02256904347 0. 2. 0. 0 17.6965130175 -1. 2. 0. 0 3.11150846518 0. 3. 0. 0 -21.5685107769 -1. 3. 0. 0 0.672852409238 0. 4. 0. 0 10.2387524315 -1. 4. 0. 0 -1.09330775541 0. 5. 0. 0 -1.20030749419 -1. 5. 0. 0 -21.1009923406 0. 1. -1. 0 21.1009923406 0. 1. 0. 0 1.0 0. 0. 1. 0 -1.0 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 methane of Vogel et al. (2000). ? ?``````````````````````````````````````````````````````````````````````````````` ?Vogel, E., Wilhelm, J., Kuechenmeister, C., and Jaesche, M., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 5 !Number of terms 0.215309028 0 !Coefficient, power of Tstar -0.46256942 1 0.051313823 2 0.030320660 3 -0.0070047029 4 @ETA !---Viscosity--- VS2 !Pure fluid viscosity model for methane 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. ? All temperatures on IPTS-68 ? ?The uncertainty in viscosity is 2%, except in the critical region which is 5%. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] CI2 !Pointer to collision integral model 0.368 !Lennard-Jones coefficient sigma [nm] 168.0 !Lennard-Jones coefficient epsilon/kappa [K] 0.1069188 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12 0.5 !Exponent in Eq 19 for T 0.16969859271 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1) -0.013337234608 !Fv(2) 1.4 !Fv(3) 168.0 !Fv(4) -16.20427429 !Coefficients for residual viscosity, eqs (22 - 25) 427.0589027 !Ev(2) 14.02596278 !Ev(3) -3916.837745 !Ev(4) -0.0347709909 !Ev(5) 21.36542674 !Ev(6) 1436.802482 !Ev(7) 10.15 !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 methane of Younglove and Ely (1987). ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., ? "Tables for the Thermophysical Properties of Methane," ? NIST Technical Note 1325, 1989. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 !Number of terms -3.0328138281 0 16.918880086 0 -37.189364917 0 41.288861858 0 -24.615921140 0 8.9488430959 0 -1.8739245042 0 0.20966101390 0 -0.009657043707 0 ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for methane 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. ! 3 !Number of terms in surface tension model 190.564 !Critical temperature used in fit (dummy) 0.03825 1.191 !Sigma0 and n -0.006024 5.422 -0.0007065 0.6161 #DE !---Dielectric constant--- DE3 !Dielectric constant model for methane 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 0 2 4 0 0 0 !Number of terms in dielectric constant model 6.5443 0. 1. 0. !Coefficient, T exp, D exp 0.0133 1. 1. 0. 8.4578 0. 2. 0. 3.7196 1. 2. 0. -352.97 0. 3. 0. -100.65 1. 3. 0. #MLT !---Melting line--- ML1 !Melting line model for methane of Setzmann and Wagner (1991). :DOI: 10.1063/1.555898 ? ?``````````````````````````````````````````````````````````````````````````````` ?Setzmann, U. and Wagner, W., ? "A New Equation of State and Tables of Thermodynamic Properties for Methane ? Covering the Range from the Melting Line to 625 K at Pressures up to 1000 MPa," ? J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 0. ! 0. ! 90.6941 11.696 !Reducing temperature and pressure 5 0 0 0 0 0 !Number of terms in melting line equation 1.0 0.0 !Coefficients and exponents 24756.8 1.85 -7366.02 2.1 -24756.8 0.0 7366.02 0.0 #SBL !---Sublimation line--- SB3 !Sublimation line model for methane of Lemmon (2002). :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W., 2002. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 90.6941 !Upper temperature limit [K] 0. ! 0. ! 90.6941 11.696 !Reducing temperature and pressure 0 1 0 0 0 0 !Number of terms in sublimation line equation -12.84 1. !Coefficients and exponents #PS !---Vapor pressure--- PS5 !Vapor pressure equation for methane of Setzmann and Wagner (1991). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ! 190.564 4599.2 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -6.036219 1.0 1.409353 1.5 -0.4945199 2.0 -1.443048 4.5 #DL !---Saturated liquid density--- DL4 !Saturated liquid density equation for methane of Setzmann and Wagner (1991). ? ?``````````````````````````````````````````````````````````````````````````````` ?Functional Form: D=Dc*EXP[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. ! 190.564 10.139128 !Reducing parameters 3 0 0 0 0 0 !Number of terms in equation 1.9906389 1.062 -0.78756197 1.5 0.036976723 7.5 #DV !---Saturated vapor density--- DV4 !Saturated vapor density equation for methane of Setzmann and Wagner (1991). ? ?``````````````````````````````````````````````````````````````````````````````` ?Functional Form: D=Dc*EXP[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. ! 190.564 10.139128 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -1.8802840 1.062 -2.8526531 2.5 -3.0006480 4.5 -5.2511690 7.5 -13.191859 12.5 -37.553961 23.5 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890 !Can't have two vs1 models in at the same time so put Friend here !It is limited to low p @ETA !Viscosity model specification VS1 pure fluid viscosity model of Friend et al. (1989). ? ?``````````````````````````````````````````````````````````````````````````````` ?Friend, D.G., Ely, J.F., and Ingham, H., ? "Tables for the Thermophysical Properties of Methane," ? NIST Technical Note 1325, 1989. ? ?The uncertainty in viscosity is 0.5% between 270 and 600 K, and 1% above ? 600 K. Below 270 K, the uncertainty is 2%. ? !``````````````````````````````````````````````````````````````````````````````` 90.6941 !Lower temperature limit [K] 625.0 !Upper temperature limit [K] 1000000.0 !Upper pressure limit [kPa] 40.072 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI2 !Pointer to reduced effective collision cross-section model 0.36652 !Lennard-Jones coefficient sigma [nm] 174.0 !Lennard-Jones coefficient epsilon/kappa [K] 174. 10.0 !Reducing parameters for T, eta 0.14105376 0.5 !Chapman-Enskog term 0 !Number of terms for initial density dependence 0 0 9 3 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential 190.551 10.139 12.149 !Reducing parameters for T, rho, eta 0.41250137 0. 1. 0. 0 -0.14390912 -1. 1. 0. 0 0.10366993 0. 2. 0. 0 0.40287464 -1. 2. 0. 0 -0.24903524 -1.5 2. 0. 0 -0.12953131 0. 3. 0. 0 0.06575776 -2. 3. 0. 0 0.02566628 0. 4. 0. 0 -0.03716526 -1. 4. 0. 0 1.0 0. 0. 0. 0 -0.38798341 0. 1. 0. 0 0.03533815 -1. 1. 0. 0 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)