self.omega = omega
self.HEOS = HEOS
# Store the propoerties in a dict of CP_fluid instances
coolprop_fluids = {}
if has_CoolProp:
for CASRN in coolprop_dict:
HEOS = AbstractState("HEOS", CASRN)
coolprop_fluids[CASRN] = CP_fluid(
Tmin=HEOS.Tmin(),
Tmax=HEOS.Tmax(),
Pmax=HEOS.pmax(),
has_melting_line=HEOS.has_melting_line(),
Tc=HEOS.T_critical(),
Pc=HEOS.p_critical(),
Tt=HEOS.Ttriple(),
omega=HEOS.acentric_factor(),
HEOS=HEOS)
def CoolProp_T_dependent_property(T, CASRN, prop, phase):
r'''Calculates a property of a chemical in either the liquid or gas phase
as a function of temperature only. This means that the property is
either at 1 atm or along the saturation curve.
Parameters
----------
T : float
Temperature of the fluid [K]
CASRN : str
self.Pmax = Pmax
self.has_melting_line = has_melting_line
self.Tc = Tc
self.Pc = Pc
self.Tt = Tt
self.omega = omega
self.HEOS = HEOS
# Store the propoerties in a dict of CP_fluid instances
coolprop_fluids = {}
if has_CoolProp:
for CASRN in coolprop_dict:
HEOS = AbstractState("HEOS", CASRN)
coolprop_fluids[CASRN] = CP_fluid(Tmin=HEOS.Tmin(), Tmax=HEOS.Tmax(), Pmax=HEOS.pmax(),
has_melting_line=HEOS.has_melting_line(), Tc=HEOS.T_critical(), Pc=HEOS.p_critical(),
Tt=HEOS.Ttriple(), omega=HEOS.acentric_factor(), HEOS=HEOS)
def CoolProp_T_dependent_property(T, CASRN, prop, phase):
r'''Calculates a property of a chemical in either the liquid or gas phase
as a function of temperature only. This means that the property is
either at 1 atm or along the saturation curve.
Parameters
----------
T : float
Temperature of the fluid [K]
CASRN : str
CAS number of the fluid
prop : str
self.omega = omega
self.HEOS = HEOS
# Store the propoerties in a dict of CP_fluid instances
coolprop_fluids = {}
if has_CoolProp:
for CASRN in coolprop_dict:
HEOS = AbstractState("HEOS", CASRN)
coolprop_fluids[CASRN] = CP_fluid(
Tmin=HEOS.Tmin(),
Tmax=HEOS.Tmax(),
Pmax=HEOS.pmax(),
has_melting_line=HEOS.has_melting_line(),
Tc=HEOS.T_critical(),
Pc=HEOS.p_critical(),
Tt=HEOS.Ttriple(),
omega=HEOS.acentric_factor(),
HEOS=HEOS)
class MultiCheb1D(object):
'''Simple class to store set of coefficients for multiple chebshev
approximations and perform calculations from them.
'''
def __init__(self, points, coeffs):
self.points = points
self.coeffs = coeffs
self.N = len(points) - 1
def __call__(self, x):
def __init__(self, symbol="N2", T=530.0, P=1000.0, child=1):
'''Init generic Fluid'''
self.symbol = symbol.upper()
# http://www.coolprop.org/_static/doxygen/html/class_cool_prop_1_1_abstract_state.html
AS = AbstractState("HEOS", self.symbol)
self.AS = AS
self.name = AS.name()
self.T = T
self.P = P
self.child = child
Tsi = TSI_fromEng(T)
Psi = PSI_fromEng(P)
AS.update(CP.PT_INPUTS, Psi, Tsi)
self.WtMol = AS.molar_mass() * 1000.0
self.Tc = Teng_fromSI(AS.T_critical())
self.Pc = Peng_fromSI(AS.p_critical())
self.Dc = Deng_fromSI(AS.rhomass_critical())
self.Ttriple = Teng_fromSI(AS.Ttriple())
try:
self.Tfreeze = Teng_fromSI(AS.T_freeze())
except:
self.Tfreeze = self.Ttriple
self.Tmin = Teng_fromSI(AS.Tmin())
self.Tmax = Teng_fromSI(AS.Tmax())
#self.Pmin = Peng_fromSI( AS.pmin() ) # missing from AbstractState
self.Pmax = Peng_fromSI(AS.pmax())
dcIdeal = self.Pc * self.WtMol / self.Tc / 10.729
self.Zc = dcIdeal / self.Dc
try:
TnbpSI = PropsSI("T", "P", 101325, "Q", Q_LIQUID, self.symbol)
self.good_nbp = True
self.Tnbp = Teng_fromSI(TnbpSI)
except:
#print('WARNING... "%s" failed Normal Boiling Point Calculation.'%self.symbol)
Ttriple = PropsSI(self.symbol, 'Ttriple')
#print(' Using Triple Point = %g degK as Tref'%Ttriple)
self.good_nbp = False
self.Tnbp = 'N/A'
if self.good_nbp:
if self.Tnbp < 536.67:
self.Tref = self.Tnbp # if NBP is low, use NBP as ref
else:
self.Tref = 536.67 # 536.67R = (SATP, Standard Ambient T P) = 77F, 25C
else:
self.Tref = Teng_fromSI(Ttriple) + 0.1
self.Pref = 14.7
#print( 'About to call setTP #1 with Tref, Pref=',self.Tref,self.Pref )
self.setTP(self.Tref, self.Pref)
#print( 'Back from call setTP')
self.Href = self.H
#print( 'About to call setTP #2')
self.setTP(T, P)
#print( 'Back from call setTP')
if child == 1:
self.dup = EC_Fluid(symbol=self.symbol,
T=self.T,
P=self.P,
child=0)
self.calcdFreezePt = 0
#fluid = "R407C"
#fluid = "R32[0.381109419953993]&R125[0.179558888662016]&R134A[0.439331691383991]"
#fluid = "R32[0.40]&R125[0.15]&R134A[0.45]"
fluids = ["R32","R125","R134a"]
moles = [0.381109419953993,0.179558888662016,0.439331691383991]
for backend in ["HEOS","REFPROP"]:
state = AbstractState(backend, '&'.join(fluids))
state.set_mole_fractions(moles)
print(state.get_mole_fractions())
print(state.get_mass_fractions())
try:
print("Normal routines")
print(state.T_critical())
print(state.p_critical())
print(True)
except:
try:
print("Routine for all points")
states = state.all_critical_points()
for crit_state in states:
print(crit_state.T)
print(crit_state.p)
print(crit_state.stable)
except:
print("All failed")
print("\n-----------------\n")
# import numpy as np
#fluid = "R407C"
#fluid = "R32[0.381109419953993]&R125[0.179558888662016]&R134A[0.439331691383991]"
#fluid = "R32[0.40]&R125[0.15]&R134A[0.45]"
fluids = ["R32", "R125", "R134a"]
moles = [0.381109419953993, 0.179558888662016, 0.439331691383991]
for backend in ["HEOS", "REFPROP"]:
state = AbstractState(backend, '&'.join(fluids))
state.set_mole_fractions(moles)
print(state.get_mole_fractions())
print(state.get_mass_fractions())
try:
print("Normal routines")
print(state.T_critical())
print(state.p_critical())
print(True)
except:
try:
print("Routine for all points")
states = state.all_critical_points()
for crit_state in states:
print(crit_state.T)
print(crit_state.p)
print(crit_state.stable)
except:
print("All failed")
print("\n-----------------\n")
# import numpy as np
def get_critical_state(
state: CoolProp.AbstractState) -> CoolProp.AbstractState:
"""Create a new state instance and update it with the critical point data
Parameters
----------
state : CoolProp.AbstractState
Returns
-------
CoolProp.AbstractState
"""
crit_state = CP.PyCriticalState()
crit_state.T = np.nan
crit_state.p = np.nan
crit_state.rhomolar = np.nan
crit_state.stable = False
try:
crit_state.T = state.T_critical()
crit_state.p = state.p_critical()
crit_state.rhomolar = state.rhomolar_critical()
crit_state.stable = True
except:
try:
for crit_state_tmp in state.all_critical_points():
if crit_state_tmp.stable and (crit_state_tmp.T > crit_state.T
or
not np.isfinite(crit_state.T)):
crit_state.T = crit_state_tmp.T
crit_state.p = crit_state_tmp.p
crit_state.rhomolar = crit_state_tmp.rhomolar
crit_state.stable = crit_state_tmp.stable
except:
raise ValueError("Could not calculate the critical point data.")
new_state = CoolProp.AbstractState(state.backend_name(),
'&'.join(state.fluid_names()))
masses = state.get_mass_fractions()
if len(masses) > 1:
new_state.set_mass_fractions(masses)
# Uses mass fraction to work with incompressible fluids
# try: new_state.build_phase_envelope("dummy")
# except: pass
# TODO: Remove this hack ASAP
# Avoid problems with https://github.com/CoolProp/CoolProp/issues/1962
BE = state.backend_name()
FL = '&'.join(state.fluid_names())
if BE == "HelmholtzEOSBackend" and FL == "Ammonia":
crit_state.T *= 1.001
msg = ""
if np.isfinite(crit_state.rhomolar) and np.isfinite(crit_state.T):
try:
new_state.specify_phase(CoolProp.iphase_critical_point)
new_state.update(CoolProp.DmolarT_INPUTS, crit_state.rhomolar,
crit_state.T)
return new_state
except Exception as e:
msg += str(e) + " - "
pass
try:
new_state.update(CoolProp.DmolarT_INPUTS, crit_state.rhomolar,
crit_state.T)
return new_state
except Exception as e:
msg += str(e) + " - "
pass
if np.isfinite(crit_state.p) and np.isfinite(crit_state.T):
try:
new_state.specify_phase(CoolProp.iphase_critical_point)
new_state.update(CoolProp.PT_INPUTS, crit_state.p, crit_state.T)
return new_state
except Exception as e:
msg += str(e) + " - "
pass
try:
new_state.update(CoolProp.PT_INPUTS, crit_state.p, crit_state.T)
return new_state
except Exception as e:
msg += str(e) + " - "
pass
raise ValueError("Could not calculate the critical point data. " + msg)
