935 lines
47 KiB
Plaintext
935 lines
47 KiB
Plaintext
Carbon dioxide !Short name
|
|
124-38-9 !CAS number
|
|
Carbon dioxide !Full name
|
|
CO2 !Chemical formula {CO2}
|
|
R-744 !Synonym
|
|
44.0098 !Molar mass [g/mol]
|
|
216.592 !Triple point temperature [K]
|
|
194.686 !Normal boiling point [K]
|
|
304.1282 !Critical temperature [K]
|
|
7377.3 !Critical pressure [kPa]
|
|
10.6249 !Critical density [mol/L]
|
|
0.22394 !Acentric factor (calculated by extrapolating the vapor pressure curve beyond the triple point temperature)
|
|
0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
|
|
IIR !Default reference state
|
|
10.0 !Version number
|
|
1013 !UN Number :UN:
|
|
other !Family :Family:
|
|
0.0 !Heating value (upper) [kJ/mol] :Heat:
|
|
1. !GWP (IPCC 2007) :GWP:
|
|
40000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
|
|
A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
|
|
1S/CO2/c2-1-3 !Standard InChI String :InChi:
|
|
CURLTUGMZLYLDI-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
|
|
???? !Alternative fluid for mixing rules :AltID:
|
|
77c8bee0 !Hash number from InChI Key :Hash:
|
|
|
|
|
|
|
|
|
|
!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
|
|
! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
|
|
! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
|
|
! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
|
|
! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
|
|
! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
|
|
! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
|
|
! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
|
|
! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
|
|
! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
|
|
! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
|
|
! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
|
|
! end of the fluid file is marked with @END. Anything below that is ignored.
|
|
|
|
|
|
! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado
|
|
! 06-07-96 MM, Original version.
|
|
! 09-06-96 MM, Add surface tension fit of Rathjen and Straub.
|
|
! 10-09-96 MM, Replace temporary Cp0 fit with function of Ely et al.
|
|
! 06-08-97 MM, Add transport formulation of Vesovic (1990).
|
|
! 07-11-97 MM, Revert to ECS transport until Vesovic model fully implemented.
|
|
! 07-27-98 EWL, Add Span equation of state.
|
|
! 11-17-98 MM, Incorrect coeff in TCX dilute gas: 7.537.d0, not 7.737.d1.
|
|
! 12-04-98 MM, Add fit of thermal conductivity shape factor in ECS method.
|
|
! 03-09-99 EWL, Add CO2 viscosity equation of Fenghour et al. (1998).
|
|
! 11-01-99 EWL, Add Span 12 term short equation of state.
|
|
! 01-25-00 EWL, Change the limits of the TCX eq. to match the EOS. Before, there was a jump as the program switched from Vesovic to ECS. The Vesovic equation extrapolates well outside its boundaries.
|
|
! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
|
|
! 09-14-06 EWL, Change upper T limit from 1100 to 2000 K.
|
|
! 03-05-07 MLH, Add FT viscosity model of Quinones-Cisneros and Deiters.
|
|
! 01-28-07 EWL, Change normal boiling point temperature to match that from Span.
|
|
! 12-14-09 MT, Add ancillary equations.
|
|
! 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).
|
|
! 12-29-15 MLH, Add new CO2 viscosity model, new thermal conductivity coeff fit 12.29.15.
|
|
! 06-08-16 EWL, Fix wrong sign on first hyperbolic term of the Kunz PHK equation.
|
|
! 03-21-17 MLH, Revise CO2 viscosity model to match final published manuscript.
|
|
! 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 carbon dioxide of Span and Wagner (1996).
|
|
:TRUECRITICALPOINT: 304.1282 10.6249063 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
|
|
:DOI: 10.1063/1.555991
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.,
|
|
? "A New Equation of State for Carbon Dioxide Covering the Fluid Region
|
|
? from the Triple-Point Temperature to 1100 K at Pressures up to 800 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 25(6):1509-1596, 1996.
|
|
?
|
|
?The estimated uncertainties at pressures up to 30 MPa and temperatures up
|
|
? to 523 K range from 0.03% to 0.05% in density, 0.03% (in the vapor)
|
|
? to 1% in the speed of sound (0.5% in the liquid) and 0.15% (in the
|
|
? vapor) to 1.5% (in the liquid) in heat capacity. Special interest has
|
|
? been focused on the description of the critical region and the
|
|
? extrapolation behavior of the formulation (to the limits of chemical
|
|
? stability).
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
CPP !Pointer to Cp0 model
|
|
44.0098 !Molar mass [g/mol]
|
|
216.592 !Triple point temperature [K]
|
|
517.95 !Pressure at triple point [kPa]
|
|
26.777 !Density at triple point [mol/L]
|
|
194.686 !Normal boiling point temperature [K]
|
|
0.22394 !Acentric factor
|
|
304.1282 7377.3 10.6249063 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
304.1282 10.6249063 !Reducing parameters [K, mol/L]
|
|
8.31451 !Gas constant [J/mol-K]
|
|
34 4 8 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.388568232032 0.0 1. 0. !a(i),t(i),d(i),l(i)
|
|
2.93854759427 0.75 1. 0.
|
|
-5.58671885349 1.0 1. 0.
|
|
-0.767531995925 2.0 1. 0.
|
|
0.317290055804 0.75 2. 0.
|
|
0.548033158978 2.0 2. 0.
|
|
0.122794112203 0.75 3. 0.
|
|
2.16589615432 1.5 1. 1.
|
|
1.58417351097 1.5 2. 1.
|
|
-0.231327054055 2.5 4. 1.
|
|
0.0581169164314 0.0 5. 1.
|
|
-0.553691372054 1.5 5. 1.
|
|
0.489466159094 2.0 5. 1.
|
|
-0.0242757398435 0.0 6. 1.
|
|
0.0624947905017 1.0 6. 1.
|
|
-0.121758602252 2.0 6. 1.
|
|
-0.370556852701 3.0 1. 2.
|
|
-0.0167758797004 6.0 1. 2.
|
|
-0.11960736638 3.0 4. 2.
|
|
-0.0456193625088 6.0 4. 2.
|
|
0.0356127892703 8.0 4. 2.
|
|
-0.00744277271321 6.0 7. 2.
|
|
-0.00173957049024 0.0 8. 2.
|
|
-0.0218101212895 7.0 2. 3.
|
|
0.0243321665592 12.0 3. 3.
|
|
-0.0374401334235 16.0 3. 3.
|
|
0.143387157569 22.0 5. 4.
|
|
-0.134919690833 24.0 5. 4.
|
|
-0.0231512250535 16.0 6. 4.
|
|
0.0123631254929 24.0 7. 4.
|
|
0.00210583219729 8.0 8. 4.
|
|
-0.000339585190264 2.0 10. 4.
|
|
0.00559936517716 28.0 4. 5.
|
|
-0.000303351180556 14.0 8. 6.
|
|
-213.654886883 1.0 2. 2. 2. -25.0 -325.0 1.16 1.0 0. 0. 0.
|
|
26641.5691493 0.0 2. 2. 2. -25.0 -300.0 1.19 1.0 0. 0. 0.
|
|
-24027.2122046 1.0 2. 2. 2. -25.0 -300.0 1.19 1.0 0. 0. 0.
|
|
-283.41603424 3.0 3. 2. 2. -15.0 -275.0 1.25 1.0 0. 0. 0.
|
|
212.472844002 3.0 3. 2. 2. -20.0 -275.0 1.22 1.0 0. 0. 0.
|
|
-0.666422765408 0.0 1. 2. 2. 0.875 0.3 0.7 10.0 275.0 0.3 3.5
|
|
0.726086323499 0.0 1. 2. 2. 0.925 0.3 0.7 10.0 275.0 0.3 3.5
|
|
0.0550686686128 0.0 1. 2. 2. 0.875 0.3 0.7 12.5 275.0 1.0 3.0
|
|
|
|
|
|
#AUX !---Auxiliary function for Cp0
|
|
CPP !Ideal gas heat capacity function for carbon dioxide of Span and Wagner (1996).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W., 1996.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
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
|
|
3.5 0.0
|
|
1.99427042 958.49956
|
|
0.621052475 1858.80115
|
|
0.411952928 2061.10114
|
|
1.04028922 3443.89908
|
|
0.0832767753 8238.20035
|
|
|
|
|
|
#AUX !---Auxiliary function for PX0
|
|
PX0 !Helmholtz energy ideal-gas function for carbon dioxide of Span and Wagner (1996).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W., 1996.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
1 2 5 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
|
|
2.5 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
-6.124871063353245 0.0 !aj, ti for [ai*tau**ti] terms
|
|
5.1155963185961815 1.0 !aj, ti for [ai*tau**ti] terms
|
|
1.99427042 958.49956 !aj, ti for [ai*log(1-exp(-ti/T)] terms
|
|
0.621052475 1858.80115
|
|
0.411952928 2061.10114
|
|
1.04028922 3443.89908
|
|
0.0832767753 8238.20035
|
|
|
|
|
|
|
|
|
|
--------------------------------------------------------------------------------
|
|
|
|
@EOS !---Equation of state---
|
|
FEK !Helmholtz equation of state for carbon dioxide 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.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
1100.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
PHK !Pointer to Cp0 model
|
|
44.0095 !Molar mass [g/mol]
|
|
216.592 !Triple point temperature [K]
|
|
517.94 !Pressure at triple point [kPa]
|
|
26.78 !Density at triple point [mol/L]
|
|
185.36 !Normal boiling point temperature [K]
|
|
0.225 !Acentric factor
|
|
304.1282 7377.3 10.624978698 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
304.1282 10.624978698 !Reducing parameters [K, mol/L]
|
|
8.314472 !Gas constant [J/mol-K]
|
|
22 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.52646564804653 0.0 1. 0.
|
|
-1.4995725042592 1.25 1. 0.
|
|
0.27329786733782 1.625 2. 0.
|
|
0.12949500022786 0.375 3. 0.
|
|
0.15404088341841 0.375 3. 1.
|
|
-0.58186950946814 1.375 3. 1.
|
|
-0.18022494838296 1.125 4. 1.
|
|
-0.095389904072812 1.375 5. 1.
|
|
-0.0080486819317679 0.125 6. 1.
|
|
-0.03554775127309 1.625 6. 1.
|
|
-0.28079014882405 3.75 1. 2.
|
|
-0.082435890081677 3.5 4. 2.
|
|
0.010832427979006 7.5 1. 3.
|
|
-0.0067073993161097 8.0 1. 3.
|
|
-0.0046827907600524 6.0 3. 3.
|
|
-0.028359911832177 16.0 3. 3.
|
|
0.019500174744098 11.0 4. 3.
|
|
-0.21609137507166 24.0 5. 5.
|
|
0.43772794926972 26.0 5. 5.
|
|
-0.22130790113593 28.0 5. 5.
|
|
0.015190189957331 24.0 5. 6.
|
|
-0.0153809489533 26.0 5. 6.
|
|
|
|
|
|
@AUX !---Auxiliary function for PH0
|
|
PHK !Ideal gas Helmholtz form for carbon dioxide 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.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
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
|
|
2.50002 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
11.925152758 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-16.118762264 1.0
|
|
1.06044 2.844425476 !aj, ti for cosh and sinh terms
|
|
-0.01393 1.12159609
|
|
2.04452 3.022758166
|
|
2.03366 1.589964364
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
BWR !MBWR equation of state for carbon dioxide of Ely et al. (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Ely, J.F., Magee, J.W., and Haynes, W.M.,
|
|
? "Thermophysical properties for special high CO2 content mixtures,"
|
|
? Research Report RR-110, Gas Processors Association, Tulsa, OK, 1987.
|
|
?
|
|
?Note: This report contains both MBWR and FEQ (referred to as the Schmidt-Wagner
|
|
? equation of state in the report) equations. The FEQ (Schmidt-Wagner) will
|
|
? give slightly better numbers very close to the critical point but for most
|
|
? calculations, the MBWR is the recommended equation.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.58 !Lower temperature limit [K]
|
|
440.1 !Upper temperature limit [K]
|
|
40000.0 !Upper pressure limit [kPa]
|
|
27.778 !Maximum density [mol/L]
|
|
CP1 !Pointer to Cp0 model
|
|
44.0098 !Molar mass [g/mol]
|
|
216.58 !Triple point temperature [K]
|
|
518.2 !Pressure at triple point [kPa]
|
|
26.778 !Density at triple point [mol/L]
|
|
194.75 !Normal boiling point temperature [K]
|
|
0.22394 !Acentric factor
|
|
304.21 7384.325 10.60 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
304.21 10.60 !Reducing parameters [K, mol/L]
|
|
10.60 !gamma
|
|
0.0831434 !Gas constant [L-bar/mol-K]
|
|
32 1 !Nterm, Ncoeff per term
|
|
-0.00981851065838 0.995062267309 -22.8380160313
|
|
2818.27634529 -347001.262699 0.000394706709102
|
|
-0.32555000011 4.84320083063 -352181.542995
|
|
-0.324053603343e-4 0.0468596684665 -7.54547012075
|
|
-0.381894354016e-4 -0.0442192933859 51.6925168095
|
|
0.00212450985237 -0.261009474785e-4 -0.0888533388977
|
|
0.00155226179403 415091.00494 -11017396.7489
|
|
2919.90583344 14325460.6508 10.8574207533
|
|
-247.799657039 0.0199293590763 102.749908059
|
|
0.377618865158e-4 -0.00332276512346 0.179196707121e-7
|
|
0.945076627807e-5 -0.00123400943061
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FE1 !Helmholtz equation of state for carbon dioxide of Ely et al. (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Ely, J.F., Magee, J.W., and Haynes, W.M.,
|
|
? "Thermophysical properties for special high CO2 content mixtures,"
|
|
? Research Report RR-110, Gas Processors Association, Tulsa, OK, 1987.
|
|
?
|
|
?Note: This report contains both MBWR and FEQ (referred to as the Schmidt-Wagner
|
|
? equation of state in the report) equations. The FEQ (Schmidt-Wagner) will
|
|
? give slightly better numbers very close to the critical point but for most
|
|
? calculations, the MBWR is the recommended equation.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.58 !Lower temperature limit [K]
|
|
1000. !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
26.776 !Maximum density [mol/L]
|
|
CP1 !Pointer to Cp0 model
|
|
44.0098 !Molar mass [g/mol]
|
|
216.58 !Triple point temperature [K]
|
|
518.03 !Pressure at triple point [kPa]
|
|
26.776 !Density at triple point [mol/L]
|
|
194.75 !Normal boiling point temperature [K]
|
|
0.22394 !Acentric factor
|
|
304.13 7375.21 10.63 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
304.13 10.63 !Reducing parameters [K, mol/L]
|
|
8.31434 !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
|
|
0.485497428986 0.0 1. 0. !a(i),t(i),d(i),l(i)
|
|
-1.91900462349 1.5 1. 0.
|
|
0.451739876847 2.5 1. 0.
|
|
0.00838475229022 -0.5 2. 0.
|
|
0.310719428397 1.5 2. 0.
|
|
-0.18361956385 2.0 2. 0.
|
|
0.0448878785519 0.0 3. 0.
|
|
-0.0362211893044 1.0 3. 0.
|
|
-0.0169827491865 2.5 3. 0.
|
|
0.000803504394396 0.0 6. 0.
|
|
0.000320223641512 2.0 7. 0.
|
|
-0.658956249553e-5 5.0 7. 0.
|
|
-0.461991678692e-4 2.0 8. 0.
|
|
-0.385989029443 5.0 1. 2.
|
|
0.131878614095 6.0 1. 2.
|
|
0.109639470331 3.5 2. 2.
|
|
-0.0310044422115 5.5 2. 2.
|
|
-0.0989797992915 3.0 3. 2.
|
|
-0.0222934996927 7.0 3. 2.
|
|
-0.0225488505376 6.0 5. 2.
|
|
-0.00595661202393 8.5 6. 2.
|
|
-0.0219959964099 4.0 7. 2.
|
|
0.0140330955537 6.5 8. 2.
|
|
-0.00315424157971 5.5 10. 2.
|
|
0.00044339406042 22.0 2. 4.
|
|
-0.00487628903103 11.0 3. 4.
|
|
-0.0311643343682 18.0 3. 4.
|
|
0.0226083669848 11.0 4. 4.
|
|
0.0186651858191 23.0 4. 4.
|
|
-0.399277963883 17.0 5. 4.
|
|
0.464945130861 18.0 5. 4.
|
|
-0.0817090055061 23.0 5. 4.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP1 !Ideal gas heat capacity function for carbon dioxide of Ely et al.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Ely, J.F., Magee, J.W., and Haynes, W.M.,
|
|
? "Thermophysical properties for special high CO2 content mixtures,"
|
|
? Research Report RR-110, Gas Processors Association, Tulsa, OK, 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31441 !Reducing parameters for T, Cp0
|
|
1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
3.5 0.0
|
|
2.0 960.11 ! =omega_1 (degenerate mode--taken twice)
|
|
1.0 1932.0 ! =omega_2
|
|
1.0 3380.2 ! =omega_3
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP2 !Ideal gas heat capacity function for carbon dioxide of McCarty.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?McCarty, R.D.,
|
|
? "Correlations for the Thermophysical Properties of Carbon Dioxide,"
|
|
? Unpublished correlation, National Institute of Standards
|
|
? and Technology, Boulder, 1988.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
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
|
|
-9379061.144997 -3.0
|
|
202866.6045159 -2.0
|
|
-1595.185479613 -1.0
|
|
8.189952737742 0.0
|
|
-0.001298281615271 1.0
|
|
0.000001037209193687 2.0
|
|
-0.3399620971158e-9 3.0
|
|
0.6961565991385 30000.0
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FES !Helmholtz equation of state for carbon dioxide of Span and Wagner (2003).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.
|
|
? "Equations of State for Technical Applications. III. Results for Polar Fluids,"
|
|
? Int. J. Thermophys., 24(1):111-162, 2003. doi: 10.1023/A:1022362231796
|
|
?
|
|
?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.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
CPP !Pointer to Cp0 model
|
|
44.01 !Molar mass [g/mol]
|
|
216.592 !Triple point temperature [K]
|
|
517.86 !Pressure at triple point [kPa]
|
|
26.795 !Density at triple point [mol/L]
|
|
185.3 !Normal boiling point temperature [K]
|
|
0.225 !Acentric factor
|
|
304.1282 7377.3 10.624858 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
304.1282 10.624858 !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
|
|
0.89875108 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.1281985 1.25 1. 0.
|
|
-0.06819032 1.5 1. 0.
|
|
0.076355306 0.25 3. 0.
|
|
0.00022053253 0.875 7. 0.
|
|
0.41541823 2.375 1. 1.
|
|
0.71335657 2.0 2. 1.
|
|
0.00030354234 2.125 5. 1.
|
|
-0.36643143 3.5 1. 2.
|
|
-0.0014407781 6.5 1. 2.
|
|
-0.089166707 4.75 4. 2.
|
|
-0.023699887 12.5 2. 3.
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS7 !Pure fluid viscosity model from symbolic regression for carbon dioxide of Laesecke and Muzny (2017).
|
|
:DOI: 10.1063/1.4977429
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Laesecke, A. and Muzny, C.D.,
|
|
? "Reference Correlation for the Viscosity of Carbon Dioxide,"
|
|
? J. Phys. Chem. Ref. Data, 46, 013107, 2017.
|
|
? doi: 10.1063/1.4977429
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
NUL !Pointer to collision integral model
|
|
!
|
|
!Dilute gas function
|
|
$DG RED SUMTTHRD:1 EXP CNST * SUMTTHRD:2 + SUMTTHRD:2 SUMTTHRD:1 EXP / + SUM:1 + INV SUM:1 *
|
|
!
|
|
!Second viscosity virial function
|
|
$VV RED SUM:9 CNST *
|
|
!
|
|
!Residual function
|
|
$RF RED SUM:2 SUM:2 / SUM:1 +
|
|
!
|
|
!Coefficients
|
|
$CF
|
|
1000.0 1. 1. 0. 0 !Reducing parameters for eta, T, rho
|
|
-2.21283852168356 1. 0. 0. 0 !Dilute gas
|
|
5423856.34887691 0. 0. 0. 0
|
|
1749.35489318835 0. 0. 0. 0
|
|
-369.069300007128 0.5 0. 0. 0
|
|
-269503.247933569 0. 0. 0. 0
|
|
73145.021531826 1. 0. 0. 0
|
|
1.0 1. 0. 0. 0
|
|
5.34368649509278 0.5 0. 0. 0
|
|
1.0055 0.5 0. 0. 0
|
|
!Second viscosity virial function
|
|
1000.0 200.75967461 1. 0. 0 !Reducing parameters for eta, T, rho
|
|
-19.572881 -0.0 0. 0. 0
|
|
219.73999 -0.25 0. 0. 0
|
|
-1015.3226 -0.5 0. 0. 0
|
|
2471.0125 -0.75 0. 0. 0
|
|
-3375.1717 -1.0 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
|
|
3.2634491775779287e-5 0. 0. 0. 0 !Avogadro's number * sigma^3
|
|
!Residual function
|
|
94.3605819425392 216.592 26.77899089969 0. 0 !Reducing parameters for eta, T, rho
|
|
1.0 0. 2. 0. 0
|
|
1.0 0. 8.06282737481277 0. 0
|
|
1.0 1. 0. 0. 0
|
|
-0.121550806591497 0. 0. 0. 0
|
|
0.360603235428487 1. 3. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for carbon dioxide of Huber et al. (2016).
|
|
:DOI: 10.1063/1.4940892
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Huber, M.L., Sykioti, E.A., Assael, M.J., and Perkins, R.A.,
|
|
? "Reference Correlation of the Thermal Conductivity of Carbon Dioxide
|
|
? from the Triple Point to 1100 K and up to 200 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 45, 013102, 2016.
|
|
?
|
|
?The overall uncertainty (at the 95% confidence level) of the proposed correlation varies
|
|
? depending on the state point from a low of 1% at very low pressures below 0.1 MPa
|
|
? between 300 K and 700 K, to 5% at the higher pressures of the range of validity.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
1 4 !# terms for dilute gas function: numerator, denominator
|
|
304.1282 0.001 !Reducing parameters for T (=eps/k), tcx (orig in mW/m-K)
|
|
1.0 0.5 !Coefficient (sqrt(T*), power in T (T* in this case)
|
|
0.0151874307 0.
|
|
0.028067404 -1.
|
|
0.022856419 -2.
|
|
-0.0074162421 -3.
|
|
12 0 !# terms for background gas function: numerator, denominator
|
|
304.1282 10.6249 1. !Reducing parameters for T, rho, tcx (orig corr in kg/m**3, mW/m-K)
|
|
0.0100128 0. 1. 0.
|
|
0.0560488 0. 2. 0.
|
|
-0.081162 0. 3. 0.
|
|
0.0624337 0. 4. 0.
|
|
-0.0206336 0. 5. 0.
|
|
0.00253248 0. 6. 0.
|
|
0.00430829 1. 1. 0.
|
|
-0.0358563 1. 2. 0.
|
|
0.067148 1. 3. 0.
|
|
-0.0522855 1. 4. 0.
|
|
0.0174571 1. 5. 0.
|
|
-0.00196414 1. 6. 0.
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
|
TK3 !Simplified thermal conductivity critical enhancement for carbon dioxide of Huber et al. (2016).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Huber, M.L., Sykioti, E.A., Assael, M.J., and Perkins, R.A.,
|
|
? "Reference Correlation of the Thermal Conductivity of Carbon Dioxide
|
|
? from the Triple Point to 1100 K and up to 200 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 45, 013102, 2016.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
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)
|
|
0.15e-9 !Xi0 (amplitude) [m]
|
|
0.052 !Gam0 (amplitude) [-]
|
|
0.4e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
|
456.19 !Tref (reference temperature) [K]
|
|
|
|
|
|
|
|
|
|
********************************************************************************
|
|
|
|
@ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for carbon dioxide of Fenghour et al. (1998).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Fenghour, A., Wakeham, W.A., Vesovic, V.,
|
|
? "The Viscosity of Carbon Dioxide,"
|
|
? J. Phys. Chem. Ref. Data, 27:31-44, 1998.
|
|
?
|
|
?The uncertainty in viscosity ranges from 0.3% in the dilute gas near room
|
|
? temperature to 5% at the highest pressures.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI1 !Pointer to reduced effective collision cross-section model
|
|
1.0 !Lennard-Jones coefficient sigma [nm] (Not used for CO2)
|
|
251.196 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
1.00697 0.5 !Chapman-Enskog term
|
|
0 !Number of terms for initial density dependence
|
|
0 5 0 0 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
|
251.196 0.0227222 1.0 !Reducing parameters for T (= eps/k), rho, eta
|
|
0.004071119 0.0 1. 0. 0 ! d_11; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
|
|
0.7198037e-4 0.0 2. 0. 0 ! d_21
|
|
0.2411697e-16 -3.0 6. 0. 0 ! d_64
|
|
0.2971072e-22 0.0 8. 0. 0 ! d_81
|
|
-0.1627888e-22 -1.0 8. 0. 0 ! d_82
|
|
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 carbon dioxide.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Fenghour, A., Wakeham, W.A., Vesovic, V., 1998.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
5 !Number of terms
|
|
0.235156 0 !Coefficient, power of Tstar
|
|
-0.491266 1
|
|
0.05211155 2
|
|
0.05347906 3
|
|
-0.01537102 4
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS4 !Pure fluid generalized friction theory viscosity model for carbon dioxide of Quinones-Cisneros and Deiters (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Quinones-Cisneros, S.E. and Deiters, U.K.,
|
|
? "Generalization of the Friction Theory for Viscosity Modeling,"
|
|
? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577
|
|
?
|
|
?The uncertainty in viscosity ranges from 0.3% in the dilute gas near room
|
|
? temperature to 5% at the highest pressures.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.58 !Lower temperature limit [K]
|
|
1000.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
5 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
|
NUL !Pointer to reduced effective collision cross-section model; not used
|
|
0.3751 !Lennard-Jones coefficient sigma [nm] (not used)
|
|
251.196 !Lennard-Jones coefficient epsilon/kappa [K] (not used)
|
|
304.1282 1.0 !Reducing parameters for T, eta
|
|
0.0 0.5 !Chapman-Enskog term; not used here
|
|
69.18424 0.0 !Empirical terms for eta0
|
|
-215.8618 0.25
|
|
210.94362 0.5
|
|
-49.0494 0.75
|
|
0 !Number of terms for initial density dependence
|
|
1.19805e-4 -1.25861e-4 5.48871e-5 0. 0. ! a(0),a(1),a(2)
|
|
3.15921e-5 -2.60469e-5 7.09199e-6 0. 0. ! b(0),b(1),b(2)
|
|
1.80689e-5 -7.41742e-6 0.0 0. 0. ! c(0),c(1),c(2)
|
|
-2.31066e-9 0.0 5.42486e-10 0. 0. ! A(0),A(1),A(2)
|
|
1.04558e-8 -2.20758e-9 0.0 0. 0. ! B(0),B(1),B(2)
|
|
1.03255e-6 -8.56207e-7 3.84384e-7 0. 0. ! C(0),C(1),C(2)
|
|
0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2)
|
|
0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (R134a reference); fitted to data for carbon dioxide.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
|
|
?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
|
|
?
|
|
?THERMAL CONDUCTIVITY
|
|
? The ECS parameters for thermal conductivity were based on the data of:
|
|
? Johns, A.I., Rashid, S., Watson, J.T.R., and Clifford, A., "Thermal conductivity of argon, nitrogen, carbon dioxide at elevated temperatures and pressures," J. Chem. Soc. Faraday Trans. I, 82:2235-2246, 1986.
|
|
? Johnston, H.L. and Grilly, E.R., "The thermal conductivities of eight common gases between 80ø and 380øK," J. Chem. Phys., 14:233-238, 1946.
|
|
? Millat, J., Mustafa, M., Ross, M., Wakeham, W.A., and Zalaf, M., "The thermal conductivity of argon, carbon dioxide and nitrous oxide," Physica A, 145:461-497, 1987.
|
|
? Scott, A.C., Johns, A.I., Watson, J.T.R., and Clifford, A.A., "Thermal conductivity of carbon dioxide in the temperature range 300-348 K and pressures up to 25 MPa," J. Chem. Soc. Faraday Trans. I, 79:733-740, 1983.
|
|
? Average absolute deviations of the fit from the experimental data are:
|
|
? Johns: 0.90%; Johnston: 0.46%; Millat: 1.31%; Scott: 2.09%; Overall: 1.53%
|
|
?
|
|
?The Lennard-Jones parameters were taken from Vesovic, V., Wakeham, W.A., Olchowy, G.A., Sengers, J.V., Watson, J.T.R., and Millat, J., "The transport properties of carbon dioxide," J. Phys. Chem. Ref. Data, 19:763-808, 1990.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.58 !Lower temperature limit [K]
|
|
440.0 !Upper temperature limit [K]
|
|
40000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
FEQ R134A.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)
|
|
0.3751 !Lennard-Jones coefficient sigma [nm] for ECS method
|
|
251.196 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
|
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
|
7.0793e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
|
1.3194e-6 1. 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
|
|
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
|
0.89982 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
0.0297332 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
|
|
|
|
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
|
|
|
#STN !---Surface tension---
|
|
ST1 !Surface tension model for carbon dioxide of Mulero et al. (2012).
|
|
:DOI: 10.1063/1.4768782
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Mulero, A., Cachadiña, I., and Parra, M.I.,
|
|
? "Recommended Correlations for the Surface Tension of Common Fluids,"
|
|
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1 !Number of terms in surface tension model
|
|
304.128 !Critical temperature used in fit (dummy)
|
|
0.07863 1.254 !Sigma0 and n
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE3 !Dielectric constant model for carbon dioxide 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
|
|
7.3455 0. 1. 0. !Coefficient, T exp, D exp
|
|
0.00335 1. 1. 0.
|
|
83.93 0. 2. 0.
|
|
145.1 1. 2. 0.
|
|
-578.8 0. 2.55 0.
|
|
-1012.0 1. 2.55 0.
|
|
|
|
|
|
#MLT !---Melting line---
|
|
ML1 !Melting line model for carbon dioxide of Span and Wagner (1996).
|
|
:DOI: 10.1063/1.555991
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.,
|
|
? "A New Equation of State for Carbon Dioxide Covering the Fluid Region
|
|
? from the Triple-Point Temperature to 1100 K at Pressures up to 800 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 25(6):1509-1596, 1996.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
216.592 !Lower temperature limit [K]
|
|
1100.0 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
216.592 517.95 !Reducing temperature and pressure
|
|
1 2 0 0 0 0 !Number of terms in melting line equation
|
|
1.0 0.0 !Coefficients and exponents
|
|
1955.539 1.0
|
|
2055.4593 2.0
|
|
|
|
|
|
#SBL !---Sublimation line---
|
|
SB3 !Sublimation line model for carbon dioxide of Span and Wagner (1996).
|
|
:DOI: 10.1063/1.555991
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.,
|
|
? "A New Equation of State for Carbon Dioxide Covering the Fluid Region
|
|
? from the Triple-Point Temperature to 1100 K at Pressures up to 800 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 25(6):1509-1596, 1996.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
216.592 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
216.592 517.95 !Reducing temperature and pressure
|
|
0 3 0 0 0 0 !Number of terms in sublimation line equation
|
|
-14.740846 1. !Coefficients and exponents
|
|
2.4327015 1.9
|
|
-5.3061778 2.9
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for carbon dioxide of Span and Wagner (1996).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
304.1282 7377.3 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-7.0602087 1.0
|
|
1.9391218 1.5
|
|
-1.6463597 2.0
|
|
-3.2995634 4.0
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL4 !Saturated liquid density equation for carbon dioxide of Span and Wagner (1996).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
304.1282 10.6249 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
1.92451080 1.02
|
|
-0.62385555 1.5
|
|
-0.32731127 5.0
|
|
0.39245142 5.5
|
|
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV4 !Saturated vapor density equation for carbon dioxide of Span and Wagner (1996).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
304.1282 10.6249 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
-1.7074879 1.02
|
|
-0.8227467 1.5
|
|
-4.6008549 3.0
|
|
-10.111178 7.0
|
|
-29.742252 14.0
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
|
|
|
|
|
@TCX !Thermal conductivity model specification
|
|
TC1 pure fluid thermal conductivity model of Vesovic et al. (1990).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vesovic, V., Wakeham, W.A., Olchowy, G.A., Sengers, J.V., Watson, J.T.R., and Millat, J.,
|
|
? "The transport properties of carbon dioxide,"
|
|
? J. Phys. Chem. Ref. Data, 19:763-808, 1990.
|
|
?
|
|
?Note: Vesovic et al. use a crossover equation of state to compute derivatives
|
|
? in the critical region; the default EOS is used here. Also, their
|
|
? "simplified" critical enhancement for thermal conductivity is used.
|
|
?
|
|
?The uncertainty in thermal conductivity is less than 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
150. !216.58 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
37.24 !Maximum density [mol/L]
|
|
2 6 !# terms for dilute gas function: numerator, denominator
|
|
251.196 0.001 !Reducing parameters for T (=eps/k), tcx (orig in mW/m-K)
|
|
7.5378307 0.50 !Coefficient (=0.475598*SQRT(eps/k)), power in T (T* in this case)
|
|
0.048109652 -99. !Power -99 indicates: mult above numerator term by [1 + coeff*(Cp0 - 2.5*R)], where coeff = 0.4/R
|
|
0.4226159 0. !Denominator is Eq 30 in Vesovic
|
|
0.6280115 -1.
|
|
-0.5387661 -2.
|
|
0.6735941 -3.
|
|
-0.4362677 -6.
|
|
0.2255388 -7.
|
|
4 0 !# terms for background gas function: numerator, denominator
|
|
1.0 0.02272221 0.001 !Reducing parameters for T, rho, tcx (orig corr in kg/m**3, mW/m-K)
|
|
0.02447164 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
|
8.705605e-5 0. 2. 0.
|
|
-6.54795e-8 0. 3. 0.
|
|
6.594919e-11 0. 4. 0.
|
|
TK3 !Pointer to critical enhancement auxiliary function
|