453 lines
20 KiB
Plaintext
453 lines
20 KiB
Plaintext
m-Xylene !Short name
|
||
108-38-3 !CAS number
|
||
1,3-Dimethylbenzene !Full name
|
||
C8H10 !Chemical formula {C8H10}
|
||
m-Xylene !Synonym
|
||
106.165 !Molar mass [g/mol]
|
||
225.3 !Triple point temperature [K]
|
||
412.214 !Normal boiling point [K]
|
||
616.89 !Critical temperature [K]
|
||
3534.6 !Critical pressure [kPa]
|
||
2.665 !Critical density [mol/L]
|
||
0.326 !Acentric factor
|
||
0.30 !Dipole moment [Debye]; DIPPR DIADEM 2012
|
||
NBP !Default reference state
|
||
10.0 !Version number
|
||
???? !UN Number :UN:
|
||
aromatic !Family :Family:
|
||
4593.34 !Heating value (upper) [kJ/mol] :Heat:
|
||
1S/C8H10/c1-7-4-3-5-8(2)6-7/h3-6H,1-2H3 !Standard InChI String :InChi:
|
||
IVSZLXZYQVIEFR-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
|
||
f174a9b0 (octane) !Alternative fluid for mixing rules :AltID:
|
||
0f99ff70 !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
|
||
! 08-01-08 EWL, Original version.
|
||
! 01-11-13 MLH, Add transport.
|
||
! 04-01-13 SH, Add ancillary equations.
|
||
! 04-06-13 EWL, Add dipole moment.
|
||
! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014).
|
||
! 06-17-14 MLH, Add crit parameter block for thermal conductivity and revised ECS.
|
||
! 12-08-14 MLH, Add thermal conductivity model of Mylona et al. 2014.
|
||
! 12-07-15 MLH, Add viscosity model of Cao et al. 2016.
|
||
|
||
|
||
|
||
|
||
________________________________________________________________________________
|
||
|
||
#EOS !---Equation of state---
|
||
FEQ !Helmholtz equation of state for m-xylene of Zhou et al. (2012).
|
||
:TRUECRITICALPOINT: 616.89 2.665 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
|
||
:DOI: 10.1063/1.3703506
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Zhou, Y., Lemmon, E.W., and Wu, J.,
|
||
? "Thermodynamic Properties of o-Xylene, m-Xylene, p-Xylene, and Ethylbenzene,"
|
||
? J. Phys. Chem. Ref. Data, 41, 023103, 2012.
|
||
?
|
||
?The uncertainty of the equation of state for m-xylene in vapor pressure is
|
||
? 0.2% above 300 K. The uncertainty in saturated liquid density is 0.1%
|
||
? between 230 K and 400 K, and increases to 0.2% at higher and lower
|
||
? temperatures, due to a lack of experimental data. The uncertainty in
|
||
? density is 0.2% in the compressed-liquid region, and 1.0% elsewhere,
|
||
? including the critical and vapor regions. The uncertainty in sound speed
|
||
? in the liquid phase is estimated to be 0.5%. The uncertainty in
|
||
? saturation and isobaric heat capacity is 0.5%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
225.3 !Lower temperature limit [K]
|
||
700.0 !Upper temperature limit [K]
|
||
200000.0 !Upper pressure limit [kPa]
|
||
8.677 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
106.165 !Molar mass [g/mol]
|
||
225.3 !Triple point temperature [K]
|
||
0.003123 !Pressure at triple point [kPa]
|
||
8.677 !Density at triple point [mol/L]
|
||
412.214 !Normal boiling point temperature [K]
|
||
0.326 !Acentric factor
|
||
616.89 3534.6 2.665 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
616.89 2.665 !Reducing parameters [K, mol/L]
|
||
8.314472 !Gas constant [J/mol-K]
|
||
11 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
0.000012791017 1.0 8. 0. !a(i),t(i),d(i),l(i)
|
||
0.041063111 0.91 4. 0.
|
||
1.505996 0.231 1. 0.
|
||
-2.3095875 0.772 1. 0.
|
||
-0.46969 1.205 2. 0.
|
||
0.171031 0.323 3. 0.
|
||
-1.001728 2.7 1. 2.
|
||
-0.3945766 3.11 3. 2.
|
||
0.6970578 0.768 2. 1.
|
||
-0.3002876 4.1 2. 2.
|
||
-0.024311 0.818 7. 1.
|
||
0.815488 2.0 1. 2. 2. -1.0244 -1.66 1.1013 0.713 0. 0. 0.
|
||
-0.330647 2.9 1. 2. 2. -1.3788 -1.9354 0.6515 0.9169 0. 0. 0.
|
||
-0.123393 3.83 3. 2. 2. -0.9806 -1.0323 0.4975 0.6897 0. 0. 0.
|
||
-0.54661 0.5 3. 2. 2. -6.3563 -78.0 1.26 0.7245 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 m-xylene of Zhou et al. (2012).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Zhou, Y., Lemmon, E.W., and Wu, J., 2012.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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
|
||
2.169909 0.0
|
||
4.44312 160.0
|
||
2.862794 190.0
|
||
24.83298 1333.0
|
||
16.26077 3496.0
|
||
|
||
|
||
#AUX !---Auxiliary function for PX0
|
||
PX0 !Helmholtz energy ideal-gas function for m-xylene of Zhou et al. (2012).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Zhou, Y., Lemmon, E.W., and Wu, J., 2012.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
|
||
1.169909 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
||
12.6528905042467272 0.0 !aj, ti for [ai*tau**ti] terms
|
||
-0.4597586328446329 1.0 !aj, ti for [ai*tau**ti] terms
|
||
4.44312 160.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
|
||
2.862794 190.0
|
||
24.83298 1333.0
|
||
16.26077 3496.0
|
||
|
||
|
||
#AUX !---Auxiliary function for PH0
|
||
PH0 !Ideal gas Helmholtz form for m-xylene of Zhou et al. (2012).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Zhou, Y., Lemmon, E.W., and Wu, J., 2012.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
||
1.169909 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
||
12.652887 0.0 !aj, ti for [ai*tau**ti] terms
|
||
-0.45975624 1.0
|
||
4.44312 -0.2593655271 !aj, ti for [ai*log(1-exp(ti*tau)] terms
|
||
2.862794 -0.3079965634
|
||
24.83298 -2.1608390475
|
||
16.26077 -5.6671367667
|
||
|
||
|
||
|
||
|
||
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
||
|
||
#ETA !---Viscosity---
|
||
VS6 !Pure fluid viscosity model for m-xylene of Cao et al. (2016).
|
||
:DOI: 10.1063/1.4941241
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Cao, F.L., Meng, X.Y., Wu, J.T., and Vesovic, V.,
|
||
? "Reference Correlation of the Viscosity of Meta-Xylene from 273 K to 673 K and Up to 200 MPa,"
|
||
? J. Phys. Chem. Ref. Data, 45, 013103, 2016.
|
||
? doi: 10.1063/1.4941241
|
||
?
|
||
?The overall uncertainty of the proposed correlation varies from 1% for the viscosity
|
||
? at atmospheric pressure to 5% for the viscosity at high pressures and temperatures.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
225.3 !Lower temperature limit [K] Note: this is not the EOS lower limit
|
||
700.0 !Upper temperature limit [K]
|
||
200000.0 !Upper pressure limit [kPa]
|
||
15.0 !Maximum density [mol/L]
|
||
1 !Number of terms associated with dilute-gas function
|
||
CI3 !Pointer to reduced effective collision cross-section model
|
||
1.0 !Lennard-Jones coefficient sigma [nm] not used here
|
||
1.0 !Lennard-Jones coefficient epsilon/kappa [K] not used here
|
||
1.0 1.0 !Reducing parameters for T, eta
|
||
0.22115 1.0 !Chapman-Enskog term 0.021357*SQRT(MW)
|
||
0 !Number of terms for initial density dependence
|
||
0 10 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
|
||
616.89 2.665 1.0 !Reducing parameters for T, rho, eta
|
||
35.3949 0.0 1.0 0. 0
|
||
-46.9262 -1.0 1.0 0. 0
|
||
11.6533 -2.0 1.0 0. 0
|
||
-0.26895 0.5 7.4666667 0. 0
|
||
0.320971 0.2 7.4666667 0. 0
|
||
-0.0290018 0.5 3.9666667 0. 0
|
||
1.72866e-10 -2.7 22.6666667 0. 0
|
||
14.7728 0.5 2.2666667 0. 0
|
||
-18.9852 1.5 1.2666667 0. 0
|
||
17.1128 0.5 1.0666667 0. 0
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
#AUX !---Auxiliary function for the collision integral
|
||
CI3 !Collision integral model for m-xylene of Cao et al. (2016).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Cao, F.L., Meng, X.Y., Wu, J.T., and Vesovic, V., 2016.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
3 !Number of terms
|
||
-1.4933 0 !Coefficient, power of Tstar
|
||
473.2 -1
|
||
-57033. -2
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for m-xylene of Mylona et al. (2014).
|
||
:DOI: 10.1063/1.4901166
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mylona, S.K., Antoniadis, K.D., Assael, M.J. Huber, M.L., and Perkins, R.A.,
|
||
? "Reference Correlation of the Thermal Conductivity of o-Xylene, m-Xylene,
|
||
? p-Xylene, and Ethylbenzene from the Triple Point to 700 K and Moderate Pressures,"
|
||
? J. Phys. Chem. Ref. Data, 48, 043104, 2014.
|
||
?
|
||
?The estimated uncertainty for thermal conductivity of liquid and supercritical densities at temperatures
|
||
? from the triple point to 375 K is 3.6%, 5% at higher temperatures, and 6% for the dilute gas.
|
||
? Uncertainties in the critical region are much larger.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
225.3 !Lower temperature limit [K]
|
||
700.0 !Upper temperature limit [K]
|
||
200000.0 !Upper pressure limit [kPa]
|
||
8.677 !Maximum density [mol/L]
|
||
7 3 !# terms for dilute gas function: numerator, denominator
|
||
616.89 0.001 !Reducing parameters for T, tcx
|
||
2.42107 0.
|
||
135.22 1.
|
||
-1231.68 2.
|
||
2968.82 3.
|
||
-1079.73 4.
|
||
186.86 5.
|
||
-12.9167 6.
|
||
-8.50118 0.
|
||
31.1646 1.
|
||
0.001 2.
|
||
10 0 !# terms for background gas function: numerator, denominator
|
||
616.89 2.665 1. !Reducing parameters for T, rho, tcx
|
||
-0.0679314 0. 1. 0.
|
||
0.225778 0. 2. 0.
|
||
-0.185693 0. 3. 0.
|
||
0.0619006 0. 4. 0.
|
||
-0.00711664 0. 5. 0.
|
||
0.0592537 1. 1. 0.
|
||
-0.162626 1. 2. 0.
|
||
0.133036 1. 3. 0.
|
||
-0.0449051 1. 4. 0.
|
||
0.0056186 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 m-xylene 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: 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)
|
||
0.235e-9 !Xi0 (amplitude) [m]
|
||
0.057 !Gam0 (amplitude) [-]
|
||
0.713e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
925.3 !Tref (reference temperature) [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); fitted to limited data for m-xylene.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?*** 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
|
||
?
|
||
?VISCOSITY
|
||
? Measurements of the viscosity of benzene, toluene, and m-xylene at pressure up to 80 MPa
|
||
? Assael, M. J., Papadaki, M., Wakeham, W. A., Int. J. Thermophys., 1991, 12, 449-457 doi: 10.1007/BF00502361
|
||
?
|
||
?Estimated uncertainty in liquid phase viscosity for 303-323 K at pressures to 50 MPa approximately 5 %.
|
||
?
|
||
?THERMAL CONDUCTIVITY
|
||
? Watanabe, H., Kato, H., Thermal Conductivity and Thermal Diffusivity of Twenty-Nine Liquids: Alkenes, Cyclic (Alkanes, Alkenes, Alkadienes, Aromatics), and Deuterated Hydrocarbons J. Chem. Eng. Data, 2004, 49, 809-825
|
||
?
|
||
?Estimated uncertainty for the saturated liquid phase thermal conductivity between 258 and 330 K is 3%.
|
||
?
|
||
?The Lennard-Jones parameters were estimated with the method of Chung.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
225.3 !Lower temperature limit [K]
|
||
700.0 !Upper temperature limit [K]
|
||
200000.0 !Upper pressure limit [kPa]
|
||
8.677 !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)
|
||
0.58 !Lennard-Jones coefficient sigma [nm] for ECS method (estimated) sigma [nm] =0.809vc*(1/3)A
|
||
489.87 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method (estimated) eps/kappa [K] =Tc/1.2593
|
||
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
|
||
1.96357 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.722142 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.130396 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
|
||
0.957985 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0366063 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 m-xylene of Mulero et al. (2014).
|
||
:DOI: 10.1063/1.4878755
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A. and Cachadi<64>a, 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
|
||
616.89 !Critical temperature used in fit (dummy)
|
||
0.06445 1.256 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for m-xylene of Herrig (2013).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Herrig, S., 2013.
|
||
?
|
||
?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. !
|
||
616.89 3534.6 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.5635 1.0
|
||
1.2857 1.5
|
||
-3.2346 3.1
|
||
-1.9018 5.6
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for m-xylene of Herrig (2013).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Herrig, S., 2013.
|
||
?
|
||
?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. !
|
||
616.89 2.665 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
0.43346 0.16
|
||
3.8716 0.6
|
||
-3.0144 1.0
|
||
1.6190 1.5
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for m-xylene of Herrig (2013).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Herrig, S., 2013.
|
||
?
|
||
?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. !
|
||
616.89 2.665 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-1.1597 0.26
|
||
-6.0358 0.78
|
||
-16.712 2.6
|
||
-45.482 5.7
|
||
-98.418 11.7
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|