cis-Butene !Short name 590-18-1 !CAS number cis-2-Butene !Full name CH3-CH=CH-CH3 !Chemical formula {C4H8} (Z)-2-Butene !Synonym 56.10632 !Molar mass [g/mol] 134.3 !Triple point temperature [K] 276.87 !Normal boiling point [K] 435.75 !Critical temperature [K] 4225.5 !Critical pressure [kPa] 4.244 !Critical density [mol/L] 0.202 !Acentric factor 0.30 !Dipole moment [Debye]; DIPPR DIADEM 2012 NBP !Default reference state 10.0 !Version number 1012 !UN Number :UN: n-alkene !Family :Family: 2710.76 !Heating value (upper) [kJ/mol] :Heat: 1S/C4H8/c1-3-4-2/h3-4H,1-2H3/b4-3- !Standard InChI String :InChi: IAQRGUVFOMOMEM-ARJAWSKDSA-N !Standard InChI Key :InChiKey: 7b3b4080 (butane) !Alternative fluid for mixing rules :AltID: 411c4500 !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 ! 12-17-03 EWL, Original version. ! 10-14-04 MLH, Add family. ! 11-13-06 MLH, Add LJ parameters. ! 06-21-10 CKL, Add ancillary equations. ! 04-06-13 EWL, Add dipole moment. ! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014). ! 05-04-16 MLH, Add viscosity and thermal conductivity equations. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for cis-butene of Lemmon and Ihmels (2005). :TRUECRITICALPOINT: 435.75 4.244 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1016/j.fluid.2004.09.004 ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W. and Ihmels, E.C., ? "Thermodynamic Properties of the Butenes. Part II. Short Fundamental ? Equations of State," ? Fluid Phase Equilib., 228-229:173-187, 2005. doi: 10.1016/j.fluid.2004.09.004 ? ?The uncertainties in densities calculated with the equation of state ? are 0.1% in the liquid phase at temperatures above 270 K (rising to ? 0.5% at temperatures below 200 K), 0.2% at temperatures above the ? critical temperature and at pressures above 10 MPa, and 0.5% in the ? vapor phase, including supercritical conditions below 10 MPa. The ? uncertainty in the vapor phase may be higher than 0.5% in some regions. ? The uncertainty in vapor pressure is 0.2% between 220 and 310 K and ? 0.5% above 310 K, and the uncertainty in heat capacities is 0.5% at ? saturated liquid conditions, rising to 5% at much higher pressures and ? at temperatures above 300 K. ? !``````````````````````````````````````````````````````````````````````````````` 134.3 !Lower temperature limit [K] 525. !Upper temperature limit [K] 50000. !Upper pressure limit [kPa] 14.09 !Maximum density [mol/L] CPP !Pointer to Cp0 model 56.10632 !Molar mass [g/mol] 134.3 !Triple point temperature [K] 0.0002636 !Pressure at triple point [kPa] 14.09 !Density at triple point [mol/L] 276.87 !Normal boiling point temperature [K] 0.202 !Acentric factor 435.75 4225.5 4.244 !Tc [K], pc [kPa], rhoc [mol/L] 435.75 4.244 !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 0.77827 0.12 1. 0. !a(i),t(i),d(i),l(i) -2.8064 1.3 1. 0. 1.0030 1.74 1. 0. 0.013762 2.1 2. 0. 0.085514 0.28 3. 0. 0.00021268 0.69 7. 0. 0.22962 0.75 2. 1. -0.072442 2.0 5. 1. -0.23722 4.4 1. 2. -0.074071 4.7 4. 2. -0.026547 15.0 3. 3. 0.012032 14.0 4. 3. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for cis-butene of Lemmon and Ihmels (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W. and Ihmels, E.C., 2005. ? !``````````````````````````````````````````````````````````````````````````````` 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 3.9687 0.0 3.2375 248.0 7.0437 1183.0 11.414 2092.0 7.3722 4397.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for cis-butene of Lemmon and Ihmels (2005). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, E.W. and Ihmels, E.C., 2005. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 2.9687 1.0 !ai, ti for [ai*log(tau**ti)] terms 0.2591562202490252 0.0 !aj, ti for [ai*tau**ti] terms 2.4189874886742024 1.0 !aj, ti for [ai*tau**ti] terms 3.2375 248.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 7.0437 1183.0 11.414 2092.0 7.3722 4397.0 ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); predictive mode for cis-butene. :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** ?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension ? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018. ? doi: 10.6028/NIST.IR.8209 ? ?Estimated uncertainty is 5% for gas phase; 20% for viscosity and thermal conductivity of liquid phase. ? Liquid phase data unavailable. ? ?The Lennard-Jones parameters were estimated from Hirschfelder, J.O., Curtiss, C.F., and Bird, R.B., "Molecular Theory of Gases and Liquids," John Wiley and Sons, Inc., New York, 1245 pp, 1954. doi: 10.1002/pol.1955.120178311 ? !``````````````````````````````````````````````````````````````````````````````` 134.3 !Lower temperature limit [K] 525.0 !Upper temperature limit [K] 50000.0 !Upper pressure limit [kPa] 14.09 !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) 0.5508 !Lennard-Jones coefficient sigma [nm] 259.0 !Lennard-Jones coefficient epsilon/kappa [K] 2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 0.00102143 0. 0. 0. !Coefficient, power of T, spare1, spare2 coeff from isobutene 6.64409e-7 1. 0. 0. !Coefficient, power of T, spare1, spare2 3 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.12449 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare; coeff from isobutene -0.147034 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare 0.036655 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare 2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2 0.838527 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare; coeff from isobutene 0.0648013 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare TK3 !Pointer to critical enhancement auxiliary function #AUX !---Auxiliary function for the thermal conductivity critical enhancement TK3 !Simplified thermal conductivity critical enhancement for cis-butene of Perkins et al. (2013). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L., ? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids," ? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z ? !``````````````````````````````````````````````````````````````````````````````` 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) 1.02 !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) 0.21e-9 !Xi0 (amplitude) [m] 0.058 !Gam0 (amplitude) [-] 0.607e-9 !Qd_inverse (modified effective cutoff parameter) [m] 653.63 !Tref (reference temperature)=1.5*Tc [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for cis-butene of Mulero et al. (2014). :DOI: 10.1063/1.4878755 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A. and Cachadiņa, I., ? "Recommended Correlations for the Surface Tension of Several Fluids ? Included in the REFPROP Program," ? J. Phys. Chem. Ref. Data, 43, 023104, 2014. ? doi: 10.1063/1.4878755 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 435.75 !Critical temperature used in fit (dummy) 0.05903 1.246 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for cis-butene of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, C.K. and 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. ! 435.75 4236.0 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.0022 1.0 1.3695 1.5 -3.0509 3.2 0.10012 3.46 -1.5577 6.4 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for cis-butene 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. ! 435.75 4.244 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 4.6849 0.402 -5.4614 0.54 3.4718 0.69 5.0511 6.6 -5.0389 7.0 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for cis-butene of Lemmon (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Lemmon, C.K. and 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. ! 435.75 4.244 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -2.8918 0.4098 -5.8582 1.174 -17.443 3.11 -24.566 6.1 -29.413 7.6 -113.92 14.8 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890