Benzene !Short name 71-43-2 !CAS number Benzene !Full name C6H6 !Chemical formula {C6H6} Benzene !Synonym 78.11184 !Molar mass [g/mol] 278.674 !Triple point temperature [K]; Reid, Prausnitz, & Poling, McGraw-Hill (1987) 353.219 !Normal boiling point [K] 562.02 !Critical temperature [K] 4907.277 !Critical pressure [kPa] 3.901 !Critical density [mol/L] 0.211 !Acentric factor 0.0 !Dipole moment [Debye]; (exactly zero due to symmetry) NBP !Default reference state 10.0 !Version number 1114 !UN Number :UN: aromatic !Family :Family: 3301.43 !Heating value (upper) [kJ/mol] :Heat: 1S/C6H6/c1-2-4-6-5-3-1/h1-6H !Standard InChI String :InChi: UHOVQNZJYSORNB-UHFFFAOYSA-N !Standard InChI Key :InChiKey: cb03ba40 (hexane) !Alternative fluid for mixing rules :AltID: f2cfb460 !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 ! 11-13-98 EWL, Original version. ! 10-14-99 EWL, Add L-J parameters. ! 11-08-01 EWL, Change dmax. ! 08-08-05 EWL, Change tlow to ttrp. ! 08-18-10 EWL, Add equation of state of Thol et al. ! 08-19-10 IDC, Add ancillary equations. ! 07-10-12 MLH, Add transport. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ! 02-20-13 EWL, Add final equation of state of Thol et al. (2013). ! 04-06-13 EWL, Add dipole moment. ! 09-21-15 MLH, Add viscosity correlation of Avgeri et al. (2014). ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for benzene of Thol et al. (2015). :TRUECRITICALPOINT: 562.02 3.901 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M., Lemmon, E.W., and Span, R., ? Unpublished equation of state, but similar to the one published in: ? "Equation of State for Benzene for Temperatures from the Melting Line up to ? 725 K with Pressures up to 500 MPa," ? High Temp.-High Press., 41:81-97, 2012. ? ?The estimated uncertainties of properties calculated with the equation ? for benzene are 0.1% below 350 K and 0.2% above 350 K for saturated vapor ? pressures and liquid densities, 1% for saturated vapor densities, 0.1% for ? densities up to 350 K and 100 MPa, 0.1 - 0.5% in density above 350 K, 1% for ? the isobaric heat capacities and saturated heat capacities, and 0.5% for ? sound speeds. Deviations in the critical region are higher for all ? properties except saturated vapor pressures. ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] CPP !Pointer to Cp0 model 78.11184 !Molar mass [g/mol] 278.674 !Triple point temperature [K] 4.785 !Pressure at triple point [kPa] 11.44 !Density at triple point [mol/L] 353.219 !Normal boiling point temperature [K] 0.211 !Acentric factor 562.02 4907.277 3.901 !Tc [K], pc [kPa], rhoc [mol/L] 562.02 3.901 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 10 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.03512459 1.0 4. 0. !a(i),t(i),d(i),l(i) 2.2338 0.29 1. 0. -3.10542612 0.696 1. 0. -0.577233 1.212 2. 0. 0.25101 0.595 3. 0. -0.705518 2.51 1. 2. -0.139648 3.96 3. 2. 0.83494 1.24 2. 1. -0.331456 1.83 2. 2. -0.0279953 0.82 7. 1. 0.7099766 0.57 1. 2. 2. -1.032 -1.864 1.118 0.729 0. 0. 0. -0.3732185 2.04 1. 2. 2. -1.423 -1.766 0.639 0.907 0. 0. 0. -0.0629985 3.2 3. 2. 2. -1.071 -1.825 0.654 0.765 0. 0. 0. -0.803041 0.78 3. 2. 2. -14.2 -297.9 1.164 0.870 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 benzene of Thol et al. (2015). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M., Lemmon, E.W., and Span, R., 2015. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.94645 0.0 7.36374 4116.0 18.649 1511.0 4.01834 630.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for benzene of Thol et al. (2015). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M., Lemmon, E.W., and Span, R., 2015. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 2.94645 1.0 !ai, ti for [ai*log(tau**ti)] terms -0.673584364528315 0.0 !aj, ti for [ai*tau**ti] terms 2.5555552197611604 1.0 !aj, ti for [ai*tau**ti] terms 7.36374 4116.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 18.649 1511.0 4.01834 630.0 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for benzene of Thol et al. (2015) ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M., Lemmon, E.W., and Span, R., 2015. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 2.94645 1.0 !ai, ti for [ai*log(tau**ti)] terms -0.6740687105 0.0 !aj, ti for [ai*tau**ti] terms 2.5560188958 1.0 7.36374 -7.3235827906 !aj, ti for [ai*log(1-exp(ti*tau)] terms 18.649 -2.6885164229 4.01834 -1.1209565496 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE1 !Helmholtz equation of state for benzene of Thol et al. (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M., Lemmon, E.W., Span, R. ? "Equation of state for benzene for temperatures from the melting line up to ? 725 K with pressures up to 500 MPa," ? High Temperatures-High Pressures, 41(2):81-97, 2012. ? ?The approximate uncertainties of properties calculated with the equation ? for benzene are 0.1% below 350 K and 0.2% above 350 K for saturated vapor ? pressures and liquid densities, 1% for saturated vapor densities, 0.1% for ? densities up to 350 K and 100 MPa, 0.1 - 0.5% in density above 350 K, 1% for ? the isobaric heat capacities and saturated heat capacities, and 0.5% for ? sound speeds. Deviations in the critical region are higher for all ? properties except saturated vapor pressures. ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] CPP !Pointer to Cp0 model 78.11184 !Molar mass [g/mol] 278.674 !Triple point temperature [K] 4.783 !Pressure at triple point [kPa] 11.45 !Density at triple point [mol/L] 353.22 !Normal boiling point temperature [K] 0.211 !Acentric factor 562.02 4906.3 3.902 !Tc [K], pc [kPa], rhoc [mol/L] 562.02 3.902 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 10 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.03513062 1.0 4. 0. !a(i),t(i),d(i),l(i) 2.229707 0.3 1. 0. -3.100459 0.744 1. 0. -0.5763224 1.174 2. 0. 0.2504179 0.68 3. 0. -0.7049091 2.5 1. 2. -0.1393433 3.67 3. 2. 0.8319673 1.26 2. 1. -0.3310741 2.6 2. 2. -0.02793578 0.95 7. 1. 0.7087408 1.0 1. 2. 2. -1.032 -1.867 1.1180 0.7289 0. 0. 0. -0.3723906 2.47 1. 2. 2. -1.423 -1.766 0.6392 0.9074 0. 0. 0. -0.06267414 3.35 3. 2. 2. -1.071 -1.824 0.6536 0.7655 0. 0. 0. -0.86295 0.75 3. 2. 2. -14.35 -297.5 1.1640 0.8711 0. 0. 0. @EOS !---Equation of state--- FE2 !Helmholtz equation of state for benzene 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. ? ?The uncertainties in density for benzene are 1% in the vapor phase, 0.3% in ? the liquid phase up to 400 K (with lower uncertainties at lower temperatures), ? 1% in the liquid phase between 400 and 500 K, and 2% and rising at ? temperatures above 500 K. Near the saturation line at temperatures below 350 ? K, the liquid phase uncertainty decreases to 0.05%. The uncertainties in ? vapor pressures are 0.15% at temperatures below 380 K, and 0.5% at higher ? temperatures. The uncertainties in heat capacities and sound speeds are 2% ? in the vapor phase and 5% in the liquid phase. ? !``````````````````````````````````````````````````````````````````````````````` 278.7 !Lower temperature limit [K] 635.0 !Upper temperature limit [K] 78000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 78.108 !Molar mass [g/mol] 278.7 !Triple point temperature [K] 6.0329 !Pressure at triple point [kPa] 11.385 !Density at triple point [mol/L] 353.234 !Normal boiling point temperature [K] 0.2092 !Acentric factor 562.05 4894.0 3.9560608 !Tc [K], pc [kPa], rhoc [mol/L] 562.05 3.9560608 !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 -0.918572178424 3. 0. 0. 0. !a(i),t(i),d(i),l(i) 1.55357491575 4. 0. 0. 0. -0.356149241161 5. 0. 0. 0. 0.817273664265 0. 1. 0. 0. -3.31303917534 1. 1. 0. 0. 3.35336626528 2. 1. 0. 0. -2.56976312022 3. 1. 0. 0. 0.427304812515 4. 1. 0. 0. 0.406483484297 0. 2. 0. 0. -0.329744378187 1. 2. 0. 0. 0.208907540720 2. 2. 0. 0. 0.0777471199254 0. 3. 0. 0. -0.202621443063 1. 3. 0. 0. -0.01485803507 0. 4. 0. 0. 0.0503167715817 1. 4. 0. 0. 0.00293012717053 1. 5. 0. 0. 0.918572178424 3. 0. 2. 0.95481 -1.55357491575 4. 0. 2. 0.95481 0.356149241161 5. 0. 2. 0.95481 -0.0447029533153 3. 2. 2. 0.95481 0.957712367542 4. 2. 2. 0.95481 -1.14688433057 5. 2. 2. 0.95481 @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for benzene. ? ?``````````````````````````````````````````````````````````````````````````````` ?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. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 78.108 !Reducing parameters for T, Cp0 5 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh -0.478176 0.0 0.00618649 1.0 -0.00000380363 2.0 0.699648e-9 3.0 0.42661e-13 4.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS1 !Pure fluid viscosity model for benzene of Avgeri et al. (2014). :DOI: 10.1063/1.4892935 ? ?``````````````````````````````````````````````````````````````````````````````` ?Avgeri, S., Assael, M.J., Huber, M.L., and Perkins, R.A., ? "Reference Correlation of the Viscosity of Benzene from the Triple Point to 675 K and up to 300 MPa," ? J. Phys. Chem. Ref. Data, 43(3), 033103, 2014. doi: 10.1063/1.4892935 ? ?The correlation is valid from the triple point to 675 K, and at pressures up to 300 MPa, with the exception of ? the temperature range lower than 350 K where the pressure is restricted to 200 MPa. For the liquid phase, ? at temperatures from 288 K to 373 K and pressures up to 80 MPa, uncertainty is estimated (at a 95% confidence level) ? to be 1.8%, increasing to 3.4% at 200 MPa, and 5% at pressures up to the correlation maximum. ? For the liquid at temperatures from 373 K to 523 K, the uncertainty is 2.7% at pressures from saturation to 50 MPa, ? rising to 3.6% at 300 MPa. For temperatures above 523 K, uncertainty in the liquid phase is estimated to be 5%. ? The uncertainty for the low-density fluid phase at temperatures from 305 K to 640 K and pressures to 0.3 MPa is estimated to be 0.2%. ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function CI1 !Pointer to reduced effective collision cross-section model 0.540 !Lennard-Jones coefficient sigma [nm] 412.0 !Lennard-Jones coefficient epsilon/kappa [K] 1.0 1.0 !Reducing parameters for T, eta 0.18875509 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term] 9 !Number of terms for initial density dependence 412. 0.094826978 !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 2471.0125 -0.75 -3375.1717 -1.0 2491.6597 -1.25 -787.26086 -1.5 14.085455 -2.5 -0.34664158 -5.50 0 0 8 6 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential 562.02 3.902 1.0 !Reducing parameters for T, rho, eta (correlation in terms of uPa-s) -2.263924 0.5 1.6666666667 0. 0 ! n1 11.493352 0.5 2.6666666667 0. 0 ! n2 -90.79586 0.5 3.6666666667 0. 0 ! n3 27.4582 0.5 4.6666666667 0. 0 ! n4 -9.98945 0.5 5.6666666667 0. 0 ! n5 1.68589 1.5 1.6666666667 0. 0 ! n6 5.260067 1.5 2.6666666667 0. 0 ! n7 11.101276 1.5 4.6666666667 0. 0 ! n8 -0.205488251 0.0 0. 0. 0 ! d1 0.074757797 0.0 1. 0. 0 ! d2 -2.74872 0.0 2. 0. 0 ! d3 1.0 0.0 3. 0. 0 ! d4 -0.083078339 1.0 0. 0. 0 ! d5 -1.1113 1.0 2. 0. 0 ! d6 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) #AUX !---Auxiliary function for the collision integral CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for benzene. ? ?``````````````````````````````````````````````````````````````````````````````` ?Avgeri, S., Assael, M.J., Huber, M.L., and Perkins, R.A., 2014. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 4 !Number of terms 0.234018 0 !Coefficient, power of Tstar -0.476136 1 0.0 2 -0.015269 3 ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for benzene of Assael et al. (2012). :DOI: 10.1063/1.4755781 ? ?``````````````````````````````````````````````````````````````````````````````` ?Assael, M.J., Mihailidou, E., Huber, M.L., and Perkins, R.A., ? "Reference Correlation of the Thermal Conductivity of Benzene from the Triple Point to 725 K and up to 500 MPa," ? J. Phys. Chem. Ref. Data, 41(4), 043102, 2012. doi: 10.1063/1.4755781 ? ?Uncertainty in thermal conductivity is estimated to be less than 4.4%, for temperatures up to 725 K and pressures ? less than 350 MPa, except in the critical region where uncertainties are much larger. ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] 3 3 !# terms for dilute gas function: numerator, denominator 1.0 0.001 !Reducing parameters for T, tcx 56991.07 0. -521.44 1. 1.5449 2. 562.02 0. 9.714 1. 0.0026102 2. 10 0 !# terms for background gas function: numerator, denominator 562.02 3.9019 1. !Reducing parameters for T, rho, tcx 0.0282489 0. 1. 0. -0.0773415 0. 2. 0. 0.0714001 0. 3. 0. -0.0236798 0. 4. 0. 0.00300875 0. 5. 0. -0.0119268 1. 1. 0. 0.0833389 1. 2. 0. -0.0898176 1. 3. 0. 0.0363025 1. 4. 0. -0.00490052 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 benzene of Assael et al. (2012). ? ?``````````````````````````````````````````````````````````````````````````````` ?Assael, M.J., Mihailidou, E., Huber, M.L., and Perkins, R.A., 2012. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 0 0 0 !# terms: terms, spare, spare, spare 1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)] 0.63 !Nu (universal exponent) 1.239 !Gamma (universal exponent) 1.02 !R0 (universal amplitude) 0.065 !Z (universal exponent--not used for t.c., only viscosity) 1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1) 0.216e-9 !Xi0 (amplitude) [m] 0.0569 !Gam0 (amplitude) [-] 0.62e-9 !Qd_inverse (modified effective cutoff parameter) [m] 843.0 !Tref (reference temperature) [K] ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (C12 reference); predictive mode for benzene. ? ?``````````````````````````````````````````````````````````````````````````````` ?*** 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 ? ?Estimated uncertainty 3% for liquid in range 293 K to 350 K at pressures <180 MPa ? ?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. ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] FEQ C12.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) 0.5349 !Lennard-Jones coefficient sigma [nm] 412.3 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 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 3 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.09271 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.161324 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare 0.0486596 0. 2. 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 ******************************************************************************** @ETA !---Viscosity--- VS5 !Pure fluid viscosity model for benzene of Chung et al. (1988). ? ?``````````````````````````````````````````````````````````````````````````````` ?Uses functional form in ? Chung, T-H., Ajlan, M., Lee, L.L. and Starling, K.E. ? "Generalized Multiparameter Correlation for Nonpolar and Polar Fluid Transport Properties" ? Ind. Eng. Chem. Res. 1988, 27, 671-679. doi: 10.1021/ie00076a024 ? Parameters sigma, epsilon and w, mur, kappa fit to data. ? ?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** ** ? ?Estimated uncertainty for liquid at 298 < T < 348 K, for p < 60 MPa is ~ 3%, larger at ? higher temps and pressures. Estimated uncertainty of dilute gas at 300 < t < 620 is ~ 2% ? !``````````````````````````````````````````````````````````````````````````````` 278.674 !Lower temperature limit [K] 725.0 !Upper temperature limit [K] 500000.0 !Upper pressure limit [kPa] 11.45 !Maximum density [mol/L] 1 !Number of terms associated with dilute-gas function NUL !Pointer to reduced effective collision cross-section model; not used 0.5023 !Lennard-Jones coefficient sigma [nm] =0.809vc*(1/3)A, fit 444.37 !Lennard-Jones coefficient epsilon/kappa [K] =Tc/1.2593, fit 1.0 1.0 !Reducing parameters for T, eta 0.18875509 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term] 0 !Number of terms for initial density dependence 0.5693 0.3209 0.0642 0. 0 !w, mur, kappa for Chung, fit 0 !Additional parameters for Chung NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for benzene 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 562.02 !Critical temperature used in fit (dummy) 0.07298 1.232 !Sigma0 and n -0.0007802 0.8635 -0.0001756 0.3065 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for benzene of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 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. ! 562.02 4906.3 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.1661 1.0 2.1551 1.5 -2.0297 2.2 -4.0668 4.8 0.38092 6.2 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for benzene of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 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. ! 562.02 3.902 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 18.160 0.534 -56.879 0.686 87.478 0.84 -64.365 1.0 18.5 1.2 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for benzene of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 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. ! 562.02 3.902 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -3.1147 0.419 -4.6689 1.12 -16.161 2.8 -146.50 7.3 518.87 10.0 -827.72 12.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890 0.5349 !Lennard-Jones coefficient sigma [nm] for ECS method 412.3 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method