TyroneGit/CapMachine
1
0
Fork 0
Code Issues Pull Requests Actions Packages Projects Releases Wiki Activity

一些优化：CAN和PLC地址的优化

Browse Source
This commit is contained in:
Tyrone CT
2025-01-01 13:11:13 +08:00
parent 8b21846424
commit 26569135d3
182 changed files with 87934 additions and 261 deletions
Download Patch File Download Diff File Expand all files Collapse all files

464
CapMachine.Wpf/PPCalculation/REFPROP/FLUIDS/R1233ZDE.FLD Normal file
View File

@@ -0,0 +1,464 @@
R1233zd(E) !Short name
102687-65-0 !CAS number
trans-1-Chloro-3,3,3-trifluoro-1-propene !Full name
CF3CH=CHCl !Chemical formula {C3H2ClF3}
HFO-1233zd(E) !Synonym
130.4962 !Molar mass [g/mol]
195.15 !Triple point temperature [K]
291.413 !Normal boiling point [K]
439.6 !Critical temperature [K]
3623.7 !Critical pressure [kPa]
3.68 !Critical density [mol/L]
0.3025 !Acentric factor
1.12 !Dipole moment [Debye]; calculated by R. Gaabe, TU Braunschweig, 2017.
IIR !Default reference state
10.0 !Version number
3163 !UN Number :UN:
halocb !Family :Family:
???? !Heating value (upper) [kJ/mol] :Heat:
1. !GWP :GWP:
16000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
1S/C3H2ClF3/c4-2-1-3(5,6)7/h1-2H/b2-1+ !Standard InChI String :InChi:
LDTMPQQAWUMPKS-OWOJBTEDSA-N !Standard InChI Key :InChiKey:
40377b40 (R1234yf) !Alternative fluid for mixing rules :AltID:
bf17dfe0 !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
! 08-01-12 EWL, Original version.
! 10-15-12 EWL, Revision based on measured data to date (p-rho-T, p_sat).
! 11-16-12 MLH, Add transport predictions.
! 11-22-13 MLH, Revise surface tension model.
! 02-10-15 EWL, Update equation of state based on corrected pvt and psat data.
! 03-09-15 EWL, Add new surface tension equation of Kondou et al. (2015).
! 11-06-15 EWL, Refit ancillary equations.
! 12-01-16 MLH, Add new thermal conductivity correlation, updated ECS viscosity coeff with 2015 EOS.
! 01-26-17 MLH, Update ECS for viscosity, implement Perkins et al (2017) thermal conductivity model, update dipole moment.
! 09-14-17 MLH, Add Wen viscosity correlation
! 01-08-17 MLH, Revise ECS viscosity model including Miyara preliminary data and set as default.
________________________________________________________________________________
#EOS !---Equation of state---
FEQ !Helmholtz equation of state for R-1233zd(E) of Mondejar et al. (2015).
:TRUECRITICALPOINT: 439.6 3.68 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
:DOI: 10.1021/acs.jced.5b00348
?
?```````````````````````````````````````````````````````````````````````````````
?Mondejar, M.E., McLinden, M.O., and Lemmon, E.W.,
? "Thermodynamic Properties of trans-1-chloro-3,3,3-Trifluoropropene
? (R1233zd(E)): Vapor Pressure, P-rho-T Data, Speed of Sound Measurements
? and Equation of State,"
? J. Chem. Eng. Data, 60:2477-2489, 2015.
? doi: 10.1021/acs.jced.5b00348
?
!```````````````````````````````````````````````````````````````````````````````
195.15 !Lower temperature limit [K]
550. !Upper temperature limit [K]
100000. !Upper pressure limit [kPa]
11.41 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
130.4962 !Molar mass [g/mol]
195.15 !Triple point temperature [K]
0.2733 !Pressure at triple point [kPa]
11.404 !Density at triple point [mol/L]
291.413 !Normal boiling point temperature [K]
0.3025 !Acentric factor
439.6 3623.7 3.68 !Tc [K], pc [kPa], rhoc [mol/L]
439.6 3.68 !Reducing parameters [K, mol/L]
8.3144598 !Gas constant [J/mol-K]
10 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.0478487 1.0 4. 0. !a(i),t(i),d(i),l(i)
1.60644 0.26 1. 0.
-2.27161 1.02 1. 0.
-0.530687 0.7 2. 0.
0.169641 0.4 3. 0.
-1.85458 1.46 1. 2.
-0.321916 2.3 3. 2.
0.636411 0.66 2. 1.
-0.121482 2.7 2. 2.
-0.0262755 1.19 7. 1.
2.37362 1.62 1. 2. 2. -0.748 -1.29 0.89 0.508 0. 0. 0.
-0.901771 1.13 1. 2. 2. -1.473 -1.61 1.13 0.366 0. 0. 0.
-0.455962 1.7 3. 2. 2. -1.39 -0.8 0.7 0.38 0. 0. 0.
-0.602941 1.35 2. 2. 2. -0.86 -1.34 0.91 0.773 0. 0. 0.
-0.0594311 1.5 2. 2. 2. -1.8 -0.49 1.2 1.17 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 R-1233zd(E) of Mondejar et al. (2015).
?
?```````````````````````````````````````````````````````````````````````````````
?Mondejar, M.E., McLinden, M.O., and Lemmon, E.W., 2015.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 8.3144598 !Reducing parameters for T, Cp0
1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
4.0 0.0
11.795 630.0
8.6848 2230.0
#AUX !---Auxiliary function for PX0
PX0 !Helmholtz energy ideal-gas function for R-1233zd(E) of Mondejar et al. (2015).
?
?```````````````````````````````````````````````````````````````````````````````
?Mondejar, M.E., McLinden, M.O., and Lemmon, E.W., 2015.
?
!```````````````````````````````````````````````````````````````````````````````
1 2 2 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
-16.4562356954883171 0.0 !aj, ti for [ai*tau**ti] terms
10.095964662989191 1.0 !aj, ti for [ai*tau**ti] terms
11.795 630.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
8.6848 2230.0
--------------------------------------------------------------------------------
@EOS !---Equation of state---
FE1 !Helmholtz equation of state for R-1233zd(E) of Mondejar et al. (2012).
?
?```````````````````````````````````````````````````````````````````````````````
?Mondejar, M.E., McLinden, M.O., Lemmon, E.W.
? preliminary equation of state, 2012.
?
!```````````````````````````````````````````````````````````````````````````````
195.15 !Lower temperature limit [K]
550. !Upper temperature limit [K]
100000. !Upper pressure limit [kPa]
11.41 !Maximum density [mol/L]
CP1 !Pointer to Cp0 model
130.4961896 !Molar mass [g/mol]
195.15 !Triple point temperature [K]
0.25 !Pressure at triple point [kPa]
11.41 !Density at triple point [mol/L]
291.47 !Normal boiling point temperature [K]
0.305 !Acentric factor
439.6 3624.0 3.68 !Tc [K], pc [kPa], rhoc [mol/L]
439.6 3.68 !Reducing parameters [K, mol/L]
8.3144621 !Gas constant [J/mol-K]
10 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.0478487 1.0 4. 0. !a(i),t(i),d(i),l(i)
1.60644 0.26 1. 0.
-2.27161 1.02 1. 0.
-0.530687 0.7 2. 0.
0.169641 0.4 3. 0.
-1.85458 1.46 1. 2.
-0.321916 2.3 3. 2.
0.636411 0.66 2. 1.
-0.121482 2.7 2. 2.
-0.0262755 1.19 7. 1.
2.37362 1.62 1. 2. 2. -0.748 -1.29 0.89 0.508 0. 0. 0.
-0.901771 1.13 1. 2. 2. -1.473 -1.61 1.13 0.366 0. 0. 0.
-0.455962 1.7 3. 2. 2. -1.39 -0.8 0.7 0.38 0. 0. 0.
-0.602941 1.35 2. 2. 2. -0.86 -1.34 0.91 0.773 0. 0. 0.
-0.0594311 1.5 2. 2. 2. -1.8 -0.49 1.2 1.17 0. 0. 0.
@AUX !---Auxiliary function for Cp0
CP1 !Ideal gas heat capacity function for R-1233zd(E) of Mondejar et al. (2012).
?
?```````````````````````````````````````````````````````````````````````````````
?Mondejar, M.E., McLinden, M.O., Lemmon, E.W.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 8.3144621 !Reducing parameters for T, Cp0
1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
4.0 0.0
11.795 630.0
8.6848 2230.0
================================================================================
#TCX !---Thermal conductivity---
TC1 !Pure fluid thermal conductivity model for R-1233zd(E) of Perkins et al. (2017).
:DOI: 10.1021/acs.jced.7b00106
?
?```````````````````````````````````````````````````````````````````````````````
?Perkins, R.A., Huber, M.L., and Assael, M.J.,
? "Measurement and Correlation of the Thermal Conductivity
? of trans-1-Chloro-3,3,3-Trifluoropropene (R1233zd(E)),"
? J. Chem. Eng. Data, 62(9):2659-2665, 2017. doi: 10.1021/acs.jced.7b00106
?
!```````````````````````````````````````````````````````````````````````````````
195. !Lower temperature limit [K]
550. !Upper temperature limit [K]
100000. !Upper pressure limit [kPa]
11.5 !Maximum density [mol/L]
3 0 !# terms for dilute gas function: numerator, denominator
439.6 1. !Reducing parameters for T, tcx
-0.0140033 0.
0.037816 1.
-0.00245832 2.
12 0 !# terms for background gas function: numerator, denominator
439.6 3.68 1. !Reducing parameters for T (= Tc), rho (= Dc), tcx
0.00862816 0. 1. 0.
-0.0208988 0. 2. 0.
0.0511968 0. 3. 0.
-0.0349076 0. 4. 0.
0.00975727 0. 5. 0.
-0.000926484 0. 6. 0.
0.000914709 1. 1. 0.
-0.00407914 1. 2. 0.
0.00845668 1. 3. 0.
-0.0108985 1. 4. 0.
0.00538262 1. 5. 0.
-0.000806009 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 R-1233zd(E) 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)
0.213e-9 !Xi0 (amplitude) [m]
0.059 !Gam0 (amplitude) [-]
5.98e-10 !Qd_inverse (modified effective cutoff parameter) [m]
659.4 !Tref (reference temperature)=1.5*Tc [K]
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
@TRN !---ECS Transport---
ECS !Extended Corresponding States model (R134a reference).
:DOI: 10.6028/NIST.IR.8209
?
?```````````````````````````````````````````````````````````````````````````````
?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
?
?VISCOSITY
? Personal communication from X. Meng, unpublished data, Xi'an Xiaotong University, China, 2017.
? Personal communication from A. Miyara, unpublished data, Saga University, Japan, 2018.
?Estimated uncertainty is 4% for the liquid over 243 to 433 K at pressures to 40 MPa, rising to 10% at 100 MPa.
?Estimated uncertainty for the gas phase is 4%.
?
?THERMAL CONDUCTIVITY
? preliminary vapor phase data of R.A. Perkins, NIST, Boulder, 2012.
?
?Estimated uncertainty 20%.
?
?The Lennard-Jones parameters were estimated with the method of Chung.
?
!```````````````````````````````````````````````````````````````````````````````
195.0 !Lower temperature limit [K]
550.0 !Upper temperature limit [K]
100000.0 !Upper pressure limit [kPa]
11.5 !Maximum density [mol/L]
FEQ R134A.FLD
VS1 !Model for reference fluid viscosity
TC1 !Model for reference fluid thermal conductivity
BIG !Large molecule identifier
0.93 0. 0. 0. !Large molecule parameters
1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
0.524 !Lennard-Jones coefficient sigma [nm] for ECS method
349.1 !Lennard-Jones coefficient epsilon/kappa [K]
1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
0.00132 0. 0. 0. !Coefficient, power of T, spare1, spare2
4 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
-0.0848988 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
1.22693 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
-0.463275 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare
0.0568798 0. 3. 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---
VS1 !Pure fluid viscosity model for R-1233zd(E) of Wen et al. (2017).
?
?```````````````````````````````````````````````````````````````````````````````
?Wen, C., Meng, X., Wu, J. "Measurement and Correlation of the Viscosity of R1233zde from 243 K to 373 K and up to 40 MPa
? submitted to J. Chem. Eng. Data, 2017.
? Esimated uncertainty in the liquid phase from 240- 400 K at pressures to 40 MPa is 2%.
? No data for gas phase; estimated uncertainty 10 %
?
!```````````````````````````````````````````````````````````````````````````````
195.15 !Lower temperature limit [K]
550.0 !Upper temperature limit [K]
100000.0 !Upper pressure limit [kPa]
11.41 !Maximum density [mol/L]
1 !Number of terms associated with dilute-gas function
CI0 !Pointer to reduced effective collision cross-section model
0.5240 !Lennard-Jones coefficient sigma [nm]
349.08 !Lennard-Jones coefficient epsilon/kappa [K]
1.0 1.0 !Reducing parameters for T, eta
0.281086 0.5 !=0.02669*SQRT(MW)*fc [Chapman-Enskog term] for Chung method with 1.44 D dip
9 !Number of terms for initial density dependence
349.08 0.086645 !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 -5.5
0 1 2 5 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
439.6 3.68 1.0 !Reducing parameters for T, rho, eta (correlation in terms of uPa-s)
17.5983 0.5 0.6666666667 0. 0 !Coefficient, power of tau, del n1
-4.02103 0.5 0.6666666667 0. 0 !Coefficient, power of tau, del n2
-105.820 0.5 1.6666666667 0. 0 !Coefficient, power of tau, del n3
-10.6936 0.0 0. 0. 0 !Coefficient, power of tau, del n4
6.57574 0.0 1. 0. 0 !Coefficient, power of tau, del n5
-5.26734 1.0 0. 0. 0 !Coefficient, power of tau, del n6
1.10633 1.0 1. 0. 0 !Coefficient, power of tau, del n7
-0.959157 0.0 2. 0. 0 !Coefficient, power of tau, del n8
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
#STN !---Surface tension---
ST1 !Surface tension model for R-1233zd(E) of Kondou et al. (2015).
:DOI: 10.1016/j.ijrefrig.2015.01.005
?
?```````````````````````````````````````````````````````````````````````````````
?Kondou, C., Nagata, R., Nii, N., Koyama, S., and Higashi, Y.,
? "Surface Tension of Low GWP Refrigerants R1243zf, R1234ze(Z), and R1233zd(E),"
? Int. J. Refrig., 53:80-89, 2015.
? doi: 10.1016/j.ijrefrig.2015.01.005
?
?Critical temperature was changed to match that from the EOS.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1 !Number of terms in surface tension model
439.6 !Critical temperature used in fit (dummy)
0.06195 1.277 !Sigma0 and n
#PS !---Vapor pressure---
PS5 !Vapor pressure equation for R-1233zd(E) of Mondejar et al. (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. !
439.6 3623.7 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-7.5635 1.0
1.8668 1.5
-2.1880 2.4
-3.4571 4.5
-2.4340 14.0
#DL !---Saturated liquid density---
DL1 !Saturated liquid density equation for R-1233zd(E) of Mondejar et al. (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. !
439.6 3.68 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
7.0378 0.53
-14.550 0.85
21.707 1.2
-18.338 1.6
7.1635 2.0
#DV !---Saturated vapor density---
DV3 !Saturated vapor density equation for R-1233zd(E) of Mondejar et al. (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. !
439.6 3.68 !Reducing parameters
6 0 0 0 0 0 !Number of terms in equation
-6.1834 0.52
6.8270 0.85
-11.226 1.2
-22.406 3.4
-58.384 7.0
-146.92 15.0
@END
c 1 2 3 4 5 6 7 8
c2345678901234567890123456789012345678901234567890123456789012345678901234567890