Methanol !Short name 67-56-1 !CAS number Methanol !Full name CH3OH !Chemical formula {CH4O} Methyl alcohol !Synonym 32.04216 !Molar mass [g/mol] 175.61 !Triple point temperature [K] 337.632 !Normal boiling point [K] 512.6 !Critical temperature [K] 8103.5 !Critical pressure [kPa] 8.6 !Critical density [mol/L] 0.5625 !Acentric factor 1.7 !Dipole moment [Debye]; Reid, Prausnitz, & Poling, McGraw-Hill (1987) NBP !Default reference state 10.0 !Version number 1230 !UN Number :UN: alcohol !Family :Family: 764.09 !Heating value (upper) [kJ/mol] :Heat: 2.8 !GWP (IPCC 2007) :GWP: 1S/CH4O/c1-2/h2H,1H3 !Standard InChI String :InChi: OKKJLVBELUTLKV-UHFFFAOYSA-N !Standard InChI Key :InChiKey: 3d5f67e0 (ethanol) !Alternative fluid for mixing rules :AltID: c41aa690 !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 ! 04-06-98 EWL, Original version. ! 11-18-98 EWL, Add equation of state of Polt et al. (1992). ! 08-25-06 MLH, Add viscosity and thermal conductivity models VS0, TC1, TK3. ! 12-02-06 MLH, Update references. ! 01-23-07 MLH, Add ECS transport model. ! 11-14-07 MLH, Add Sun and Ely EOS. ! 07-05-10 CKL, Add density ancillary equations. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ! 11-26-13 MLH, Add new thermal conductivity formulation. ! 05-15-17 EWL, Change the hard coded VS0 model to the VS7 reverse Polish notation. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for methanol of de Reuck and Craven (1993). :TRUECRITICALPOINT: 513.38 8.78517 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?de Reuck, K.M. and Craven, R.J.B., ? "Methanol, International Thermodynamic Tables of the Fluid State-12," ? IUPAC, Blackwell Scientific Publications, London, 1993. ? ?The uncertainties of the equation of state are generally 0.1% in density ? and 2% in the speed of sound, except in the critical region and high pressures. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] CPP !Pointer to Cp0 model 32.04216 !Molar mass [g/mol] 175.61 !Triple point temperature [K] 0.00018629 !Pressure at triple point [kPa] 28.230 !Density at triple point [mol/L] 337.632 !Normal boiling point temperature [K] 0.5625 !Acentric factor 513.38 8215.85 8.78517 !Tc [K], pc [kPa], rhoc [mol/L] 513.38 8.78517 !Reducing parameters [K, mol/L] 8.31448 !Gas constant [J/mol-K] 36 5 8 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -2.80062505988 0. 1. 0. 0. !a(i),t(i),d(i),l(i) 12.5636372418 1. 1. 0. 0. -13.0310563173 2. 1. 0. 0. 3.2659313406 3. 1. 0. 0. -4.11425343805 1. 2. 0. 0. 3.46397741254 2. 2. 0. 0. -0.083644396759 3. 2. 0. 0. -0.369240098923 4. 2. 0. 0. 0.00313180842152 6. 2. 0. 0. 0.603201474111 0. 3. 0. 0. -0.231158593638 3. 3. 0. 0. 0.106114844945 4. 3. 0. 0. -0.0792228164995 0. 4. 0. 0. -0.422419150975e-4 7. 4. 0. 0. 0.00758196739214 1. 5. 0. 0. -0.244617434701e-4 6. 6. 0. 0. 0.115080328802e-5 7. 7. 0. 0. -12.5099747447 1. 1. 2. 1.01733510223052 27.0392835391 2. 1. 2. 1.01733510223052 -21.2070717086 3. 1. 2. 1.01733510223052 6.3279947227 4. 1. 2. 1.01733510223052 14.3687921636 1. 2. 2. 1.01733510223052 -28.7450766617 2. 2. 2. 1.01733510223052 18.5397216068 3. 2. 2. 1.01733510223052 -3.88720372879 5. 2. 2. 1.01733510223052 -4.16602487963 1. 3. 2. 1.01733510223052 5.29665875982 2. 4. 2. 1.01733510223052 0.509360272812 1. 5. 2. 1.01733510223052 -3.30257604839 2. 5. 2. 1.01733510223052 -0.311045210826 4. 5. 2. 1.01733510223052 0.273460830583 5. 5. 2. 1.01733510223052 0.518916583979 2. 6. 2. 1.01733510223052 -0.00227570803104 5. 9. 2. 1.01733510223052 0.0211658196182 9. 6. 4. 1.03497071023039 -0.0114335123221 14. 6. 4. 1.03497071023039 0.00249860798459 19. 4. 6. 1.05291203329783 -8.19291988442 0. 1. 2. 1. -4.06934040892209 3.8940745646517 1.54080254509371 0. 0. 0. 0. 0.478601004557 0. 1. 3. 1. -8.20892015621185 3.8940745646517 1.54080254509371 0. 0. 0. 0. -0.444161392885 0. 1. 2. 1. -9.15601592007471 3.8940745646517 1.54080254509371 0. 0. 0. 0. 0.17962181041 0. 1. 4. 1. -83.8326275286616 3.8940745646517 1.54080254509371 0. 0. 0. 0. -0.687602278259 0. 1. 2. 1. -16.2773616356884 3.8940745646517 1.54080254509371 0. 0. 0. 0. 2.40459848295 0. 3. 3. 1. -27.705105527215 23.0649031906293 1.08389789427588 0. 0. 0. 0. -6.88463987466 0. 3. 2. 1. -16.2773616356884 23.0649031906293 1.08389789427588 0. 0. 0. 0. 1.13992982501 0. 3. 4. 1. -264.95250181898 23.0649031906293 1.08389789427588 0. 0. 0. 0. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for methanol of de Reuck and Craven (1993). ? ?``````````````````````````````````````````````````````````````````````````````` ?de Reuck, K.M. and Craven, R.J.B., 1993. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.31448 !Reducing parameters for T, Cp0 1 7 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.9007912 0.0 10.992677 2115.01542 18.33683 1676.18569 -16.366004 1935.16717 -6.2332348 1504.97016 2.8035363 4222.83691 1.0778099 5296.17127 0.96965697 273.36934 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for methanol of de Reuck and Craven (1993). ? ?``````````````````````````````````````````````````````````````````````````````` ?de Reuck, K.M. and Craven, R.J.B., 1993. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 7 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 2.9007912 1.0 !ai, ti for [ai*log(tau**ti)] terms -4.4231521797113365 0.0 !aj, ti for [ai*tau**ti] terms 5.4815623918310443 1.0 !aj, ti for [ai*tau**ti] terms 10.992677 2115.01542 !aj, ti for [ai*log(1-exp(-ti/T)] terms 18.33683 1676.18569 -16.366004 1935.16717 -6.2332348 1504.97016 2.8035363 4222.83691 1.0778099 5296.17127 0.96965697 273.36934 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE2 !Helmholtz equation of state for methanol of Sun and Ely (2004). ? ?``````````````````````````````````````````````````````````````````````````````` ?Sun, L. and Ely, J.F., ? "Universal equation of state for engineering application: Algorithm and ? application to non-polar and polar fluids," ? Fluid Phase Equilib., 222-223:107-118, 2004. ? !``````````````````````````````````````````````````````````````````````````````` 175.59 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 40. !Maximum density [mol/L] CPP !Pointer to Cp0 model 32.04 !Molar mass [g/mol] 175.59 !Triple point temperature [K] 0.1 !Pressure at triple point [kPa] 40. !Density at triple point [mol/L] 300. !Normal boiling point temperature [K] 0.566 !Acentric factor 512.6 8104.0 8.662422 !Tc [K], pc [kPa], rhoc [mol/L] 512.6 8.662422 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 14 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms -5.24578394 1.5 1. 0. !a(i),t(i),d(i),l(i) 1.39060027 0.25 1. 0. 0.856114069 1.25 1. 0. -0.0420843418 0.25 3. 0. 3.63682442e-5 0.875 7. 0. 0.705598662 1.375 2. 0. 0.370573369 0.0 1. 1. 2.46303468 2.375 1. 1. 1.50253790 2.0 2. 1. 0.0747553687 2.125 5. 1. -0.306417876 3.5 1. 2. -0.748402758 6.5 1. 2. -0.101432849 4.75 4. 2. 0.0806830693 12.5 2. 3. @EOS !---Equation of state--- FE1 !Helmholtz equation of state for methanol 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. ? !``````````````````````````````````````````````````````````````````````````````` 298.0 !Lower temperature limit [K] 703.0 !Upper temperature limit [K] 63000.0 !Upper pressure limit [kPa] 26.0625 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 32.0 !Molar mass [g/mol] 175.61 !Triple point temperature [K] 16.803 !Pressure at triple point [kPa] 24.576 !Density at triple point [mol/L] 337.68 !Normal boiling point temperature [K] 0.5654 !Acentric factor 512.58 8103.0 8.5 !Tc [K], pc [kPa], rhoc [mol/L] 512.58 8.5 !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 -4.12043979985 3. 0. 0. 0. !a(i),t(i),d(i),l(i) 5.41210456547 4. 0. 0. 0. -0.974639417666 5. 0. 0. 0. -0.909437999343 0. 1. 0. 0. -0.143467597275 1. 1. 0. 0. 5.57052459597 2. 1. 0. 0. -6.97445416557 3. 1. 0. 0. 0.860535902136 4. 1. 0. 0. 2.44117735035 0. 2. 0. 0. -4.49073510921 1. 2. 0. 0. 2.23855290012 2. 2. 0. 0. -0.717336537940 0. 3. 0. 0. 0.876135006507 1. 3. 0. 0. 0.151777405466 0. 4. 0. 0. -0.233178058896 1. 4. 0. 0. 0.0140022534721 1. 5. 0. 0. 4.12043979985 3. 0. 2. 0.591872 -5.41210456547 4. 0. 2. 0.591872 0.974639417666 5. 0. 2. 0.591872 -0.4642672133 3. 2. 2. 0.591872 0.944015617353 4. 2. 2. 0.591872 -0.449348200461 5. 2. 2. 0.591872 @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for methanol. ? ?``````````````````````````````````````````````````````````````````````````````` ?Polt, A., Platzer, B., and Maurer, G., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 32.0 !Reducing parameters for T, Cp0 5 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 0.96422 0.0 0.0000532325 1.0 0.00000672819 2.0 -0.768411e-8 3.0 0.27522e-11 4.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS7 !Pure fluid viscosity model for methanol of Xiang et al. (2006). :DOI: 10.1063/1.2360605 ? ?``````````````````````````````````````````````````````````````````````````````` ?Xiang, H.W., Laesecke, A., and Huber, M.L., ? "A New Reference Correlation for the Viscosity of Methanol," ? J. Phys. Chem. Ref. Data, 35(4):1597-1620, 2006. ? ?Estimated uncertainty 0.6% in the dilute gas from room T to 630 K, 2% for ? the liquid at pressures up to 30 MPa between 273 and 343 K, ? 3% for pressures from 30 MPa to 100 MPa, 5% for the liquid from 100 to 500 MPa, ? 10% for 500 MPa to 800 MPa. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] NUL !Omega model ! !Variables (u0,b,gd,cf) $VR RED SUM:1 SUMEX:1 CNST * + SUMEX:1 CNST * + $VR SUM:1 SUMEX:1 CNST * + SUMEX:1 CNST * + $VR CNST * 1 + * INV CNST * TEMP SQRT * =V1 ! V1 is eta0 in Eq. 3 ! !Dilute gas $DG V1 CNST * ! !Residual function $RF RED SUM:16 CUBE SUM:1 * =V2 ! V2 is b *D under Eq. 16 $RF 1 V2 8 / - 1 V2 4 / - CUBE INV * =V3 ! V3 is g in Eq. 16 $RF SUM:1 5 - EXP 1 + INV =V4 ! V4 is f in Eq. 18 $RF RED SUMEX:1 SUM:1 * SUM:9 SUM:1 * + 1 + V1 * V4 * !Eqs. 13 and 14 $RF V3 INV V2 CNST * + CNST V3 * V2 SQR * + V1 * 1 V4 - * + V1 - !Eqs. 15 and 18 ! !Coefficients $CF 1.0 577.87 1. 0. 0 !Reducing parameters for eta, T, rho 1.16145 -0.14874 0. 0. 0 ! ai -0.77320 1. 0. 0. 0 0.52487 0. 0. 0. 0 -2.43787 1. 0. 0. 0 2.16178 0. 0. 0. 0 0.10225 -0.97346 0. 0. 0 -0.34528 1. 0. 0. 0 0.10657 0. 0. 0. 0 -2.58055 1. 0. 0. 0 -0.44557 0. 0. 0. 0 0.209304408 0. 0. 0. 0 1.3010769266e-6 0. 0. 0. 0 1.e+6 0. 0. 0. 0 1.0 512.6 8.52002486723741 0. 0 !Reducing parameters for eta, T, rho -1.181909 0. 0. 0. 0 ! di 0.5031030 -1. 0. 0. 0 -0.6268461 -2. 0. 0. 0 0.5169312 -3. 0. 0. 0 -0.2351349 -4. 0. 0. 0 0.053980235 -5. 0. 0. 0 -0.0049069617 -6. 0. 0. 0 4.018368 0. 1. 0. 0 ! ei -4.239180 0. 2. 0. 0 2.245110 0. 3. 0. 0 -0.5750698 0. 4. 0. 0 0.023021026 0. 5. 0. 0 0.025696775 0. 6. 0. 0 -0.0068372749 0. 7. 0. 0 7.2707189e-4 0. 8. 0. 0 -2.9255711e-5 0. 9. 0. 0 4. 0. 1. 0. 0 5. 0. 1. 0. 0 1.e+6 577.87 41.9517741858221 0. 0 !Reducing parameters for eta, T, rho 9.990338 -0.5 0. 0. 0 ! ci 18.6222085e-4 3. 2. 0. 0 -19.572881 0. 0. 0. 0 ! bi 219.73999 -0.25 0. 0. 0 -1015.3226 -0.5 0. 0. 0 2471.01251 -0.75 0. 0. 0 -3375.1717 -1. 0. 0. 0 2491.6597 -1.25 0. 0. 0 -787.26086 -1.5 0. 0. 0 14.085455 -2.5 0. 0. 0 -0.34664158 -5.5 0. 0. 0 1.0 0. 1. 0. 0 0.8 0. 0. 0. 0 0.761 0. 0. 0. 0 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for methanol of Sykioti et al. (2013). :DOI: 10.1063/1.4829449 ? ?``````````````````````````````````````````````````````````````````````````````` ?Sykioti, E.A., Assael, M.J., Huber, M.L., and Perkins, R.A., ? "Reference Correlation of the Thermal Conductivity of Methanol ? from the Triple Point to 660 K and up to 245 MPa," ? J. Phys. Chem. Ref. Data, 42, 043101, 2013. ? ?Estimated uncertainty in thermal conductivity is 4.4% ? except near critical where the uncertainties are larger. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 1620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] 6 5 !# terms for dilute gas function: numerator, denominator 512.6 0.001 !Reducing parameters for T, tcx -3.57796 0. !Coefficient, power in T 62.9638 1. -37.3047 2. -52.1182 3. 231.607 4. 44.1575 5. 3.33313 0. -6.08398 1. 8.18739 2. -0.261074 3. 1.0 4. 10 0 !# terms for background gas function: numerator, denominator 512.6 8.6 1. !Reducing parameters for T, rho, tcx 0.0556918 0. 1. 0. 0.112174 0. 2. 0. -0.0843893 0. 3. 0. 0.0197525 0. 4. 0. -0.0015253 0. 5. 0. 0.0104771 1. 1. 0. -0.0745272 1. 2. 0. 0.0637569 1. 3. 0. -0.0246826 1. 4. 0. 0.00434656 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 methanol 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. Thermophys., 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) 0.1487e-9 !Xi0 (amplitude) [m] 0.05283 !Gam0 (amplitude) [-] 0.7e-9 !Qd_inverse (modified effective cutoff parameter) [m]; from Kiselev et al. (2005) 768.9 !Tref (reference temperature)=1.5*Tc [K] ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); predictive mode for methanol. ? ?``````````````````````````````````````````````````````````````````````````````` ?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** ?Unpublished; uses method described in the following reference: ?Huber, M.L., Laesecke, A., and Perkins, R.A. ? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including ? a New Correlation for the Viscosity of R134a," ? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880 ? ?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. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] FEQ PROPANE.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) 0.3626 !Lennard-Jones coefficient sigma [nm] 481.8 !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 methanol of Mulero et al. (2012). :DOI: 10.1063/1.4768782 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A., Cachadiņa, 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 513.38 !Critical temperature used in fit (dummy) 0.22421 1.3355 !Sigma0 and n -0.21408 1.677 0.083233 4.4402 #MLT !---Melting line--- ML1 !Melting line model for methanol of de Reuck and Craven (1993). :DOI: 10.1016/j.fluid.2013.03.024 ? ?``````````````````````````````````````````````````````````````````````````````` ?de Reuck, K.M. and Craven, R.J.B., ? "Methanol, International Thermodynamic Tables of the Fluid State-12," ? IUPAC, Blackwell Scientific Publications, London, 1993. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 0. ! 0. ! 175.61 0.000187 !Reducing temperature and pressure 1 3 0 0 0 0 !Number of terms in melting line equation 1.0 0.0 !Coefficients and exponents 5320770000.0 1.0 4524780000.0 1.5 3.888861e+10 4.0 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for methanol of Lemmon (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. ! 513.38 8215.85 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -8.7414 1.0 1.5035 1.5 -2.8720 2.5 -0.51345 5.0 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for methanol of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, C.K. and 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. ! 513.38 8.78517 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 0.060230 0.1 18.855 0.65 -27.626 0.79 11.213 0.95 0.69039 4.4 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for methanol of Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, C.K. and Lemmon, E.W., 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. ! 513.38 8.78517 !Reducing parameters 8 0 0 0 0 0 !Number of terms in equation -3.52208 0.39 -105.223 1.7 1341.606 2.4 -2899.24 2.8 8542.128 3.8 -16947.63 4.4 10717.58 4.8 -791.782 6.7 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890 0.3626 !Lennard-Jones coefficient sigma [nm] for ECS method 481.8 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method @TCX !Thermal conductivity model specification TC1 pure fluid thermal conductivity model of Perkins 2002 ? ?``````````````````````````````````````````````````````````````````````````````` ?Unpublished preliminary correlation, NIST, MLH, Aug. 2006 ? ?Dilute gas correlation from DIPPR DIADEM 2004 v2.7.3 (dippr@byu.edu) ? functional form for excess contribution from pure fluid thermal conductivity ? model of Perkins (2002) J. Chem. Eng. Data, 47(5):1272-1279. ? ?Estimated uncertainty in thermal conductivity is 3% for the liquid at pressures up to ? 60 MPa, 5% for the gas, and estimated to be 10% in the supercritical ? region, except near critical where the uncertainties are larger. ? ?DATA SOURCES FOR THERMAL CONDUCTIVITY ? Naziev, Y. M., Bashirov, M. M., Abdulagatov, I. M. (2004), "High-temperature and high-pressure experimental thermal conductivity for the pure methanol and binary systems methanol + n-propanol, methanol + n-octanol, and methanol + n-undecanol", Fluid Phase Equilibria 226:221-235. doi: 10.1016/j.fluid.2004.08.033 ? Assael, M. J., Charitidou, E., Nieto de Castro, C. A. (1988) "Absolute measurements of the thermal conductivity of alcohols by the transient hot-wire technique", Int. J. Thermophys., 9:813 doi: 10.1007/BF00503247 ? Raal, J.D., Rijsdijk, R.L. (1981) "Measurement of Alcohol Thermal Conductivities Using a Relative Strain-Compensated Hot-Wire Method," J. Chem. Eng. Data, 26, 351 doi: 10.1021/je00026a001 ? Average absolute deviations of the fit from the experimental data are: ? Naziev et al.: 3.1% (max 30%); Assael et al.: 0.8% (max -1.7), ? Raal and Rijsdijk: 1.1% (max 3.0%) ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] 1 0 !# terms for dilute gas function: numerator, denominator 1.0 1. !Reducing parameters for T, tcx 5.7992e-7 1.7862 !Coefficient, power in T 6 0 !# terms for background gas function: numerator, denominator 513.38 8.78517 1. !Reducing parameters for T, rho, tcx 0.405435 0. 1. 0. !Coefficient, powers of T, rho, spare for future use -0.293791 1. 1. 0. -0.289002 0. 2. 0. 0.22689 1. 2. 0. 0.0579019 0. 3. 0. -0.0399576 1. 3. 0. TK3 !Pointer to critical enhancement auxiliary function @AUX !---Thermal conductivity critical enhancement model TK3 simplified thermal conductivity critical enhancement 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) [-] 0.342e-9 !qd_inverse (modified effective cutoff parameter) [m]; from Kiselev et al. (2005) 768.9 !Tref (reference temperature)=1.5*Tc [K] @ETA !Viscosity model specification VS0 pure fluid viscosity model of Xiang et al. (2006). ? ?``````````````````````````````````````````````````````````````````````````````` ?Xiang, H.W., Laesecke, A., and Huber, M.L. "A New Reference ? Correlation for the Viscosity of Methanol", ? J. Phys. Chem. Ref. Data, 35(4):1597-1620, 2006. ? ?Estimated uncertainty 0.6% in the dilute gas from room T to 630K, 2% for ? the liquid at pressures up to 30 MPA between 273 and 343 K, ? 3% for pressures from 30 MPa to 100 MPa, 5% for the liquid from 100 to 500 MPa, ? 10% for 500 MPa to 800 MPa. ? !``````````````````````````````````````````````````````````````````````````````` 175.61 !Lower temperature limit [K] 620.0 !Upper temperature limit [K] 800000.0 !Upper pressure limit [kPa] 35.57 !Maximum density [mol/L] MEO !Pointer to hardcoded viscosity model 0 1 1 0 0 0 0 0 !Number of terms for various pieces 1.0 1.0 1.0 !Reducing parameters for T, rho, eta 0. 0. 0. 0. 0 !Dilute gas coeffs 0. 0. 0. 0. 0 !Residual coeffs NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)