def setUp(self):
self.phases = ct.import_phases('KOH.xml', [
'K_solid', 'K_liquid', 'KOH_a', 'KOH_b', 'KOH_liquid',
'K2O2_solid', 'K2O_solid', 'KO2_solid', 'ice', 'liquid_water',
'KOH_plasma'
])
self.mix = ct.Mixture(self.phases)
def setUp(self):
self._gas = ct.Solution('h2o2.yaml')
self._carbon = ct.Solution('graphite.yaml')
self._mix = ct.Mixture([self._gas, self._carbon])
self._output.save(self._mix, 'foo')
self._mix.T = 500
self._output.save(self._mix, 'bar')
def compute_Zst(self):
s = self
s.gas.TPY = s.T1, s.pres, s.y1
mix = ct.Mixture([(s.gas, 1.0)])
nc1 = mix.element_moles("C")
nh1 = mix.element_moles("H")
no1 = mix.element_moles("O")
nn1 = mix.element_moles("N")
nfsp = mix.species_moles
nf = sum(nfsp)
no2_per_nfuel = (nc1 + nh1 / 4 - no1 / 2) / nf
n1 = 1
n0 = no2_per_nfuel / s.x0[s.gas.species_index("O2")]
s.gas.TPY = s.T0, s.pres, s.y0
M0 = s.gas.mean_molecular_weight
s.gas.TPY = s.T1, s.pres, s.y1
M1 = s.gas.mean_molecular_weight
s.Zst = n1 * M1 / (n0 * M0 + n1 * M1)
def doAnalysis(fuel):
gas.set_equivalence_ratio(1.0, fuel, air)
mix = ct.Mixture([(gas, 1.0), (carbon, 0.0)])
mix.T = Ti
mix.P = Pi
mix.equilibrate('HP')
products = mix.phase(0)
prodx = dict(zip(products.species_names, products.X))
fuel = fixDict(fuel)
ox = fixDict({'N2': 3.76, 'O2': 1})
inert = fixDict(prodx)
dfOut = pd.DataFrame(columns=['Xf', 'Xa', 'Xi', 'phi', 'Tad', 'Flammable'])
Xf = 0.01
haseverburned = False
while Xf <= 1.:
Xa = round(1.0 - Xf, 3)
burned = False
while Xa >= 0:
Xi = abs(round(1.00 - Xf - Xa, 3))
MMIX = collections.defaultdict(lambda: 0)
for key in gaslistfull:
MMIX[key] = Xf * fuel[key] + Xa * ox[key] + Xi * inert[key]
Tl, Tu = Tblend(MMIX)
dres = Eqq(MMIX)
if dres['phi'] > 1:
if dres['Tad'] > Tu:
Flammable = 1
burned = True
haseverburned = True
else:
Flammable = 0
else:
if dres['Tad'] > Tl:
Flammable = 1
haseverburned = True
burned = True
else:
Flammable = 0
dfOut = dfOut.append(
{
'Xf': Xf,
'Xa': Xa,
'Xi': Xi,
'phi': dres['phi'],
'Tad': dres['Tad'],
'Flammable': Flammable
},
ignore_index=True)
print(Xf, Xa, Xi, Flammable, dres['Tad'])
if sum(dfOut.iloc[-2::]['Flammable']) == 0.0:
Xa = round(Xa - 0.1, 1)
else:
Xa = round(Xa - 0.01, 3)
if haseverburned and burned:
Xf = round(Xf + 0.1, 1)
else:
Xf = round(Xf + 0.01, 3)
return dfOut
def test_properties(self):
mix = ct.Mixture([(self.phase1, 1.0), (self.phase2, 2.0)])
self.assertEqual(mix.nSpecies, self.phase1.nSpecies + self.phase2.nSpecies)
mix.temperature = 350
self.assertEqual(mix.temperature, 350)
mix.pressure = 2e5
self.assertEqual(mix.pressure, 2e5)
def run(initial, phases, equilibrate):
"""Function handling equilibrium calculations.
The function handles equilibrium calculations for both single
phases (``Solution``; single entry in *phases* argument) and multiple
phases (``Mixture``; multiple entries in *phases* argument).
Arguments:
initial (Parser): Initial condition
phases (Parser): Definition of phases
equilibrate (Parser): Arguments of ``equilibrate`` function
Returns:
Cantera `Solution` or `Mixture` object
"""
T = initial.T.m_as('kelvin')
P = initial.P.m_as('pascal')
# phases that will be included in the calculation, and their initial moles
mix_phases = []
for phase in phases.values():
if phase is None:
continue
obj = ct.Solution(phase.mechanism)
if all([key in phase
for key in ['fuel', 'oxidizer']] + ['phi' in initial]):
obj.TP = T, P
obj.set_equivalence_ratio(initial.phi, phase.fuel, phase.oxidizer)
elif 'X' in phase:
obj.TPX = T, P, phase.X
elif 'Y' in phase:
obj.TPY = T, P, phase.Y
mix_phases.append((obj, phase.get('moles')))
# equilibrate the mixture based on configuration
if len(mix_phases) > 1:
obj = ct.Mixture(mix_phases)
obj.T = T
obj.P = P
kwargs = equilibrate.raw
mode = kwargs.pop('mode')
obj.equilibrate(mode, **kwargs)
print('Tad = {:8.2f}'.format(obj.T))
return obj
def solve(self, solver, **kwargs):
n_points = 12
T = 300
P = 101325
data = np.zeros((n_points, 2+self.n_species))
phi = np.linspace(0.3, 3.5, n_points)
for i in range(n_points):
self.gas.set_equivalence_ratio(phi[i], self.fuel,
{'O2': 1.0, 'N2': 3.76})
mix = ct.Mixture(self.mix_phases)
mix.T = T
mix.P = P
# equilibrate the mixture adiabatically at constant P
mix.equilibrate('HP', solver=solver, max_steps=1000, **kwargs)
data[i,:2] = (phi[i], mix.T)
data[i,2:] = mix.species_moles
self.compare(data, pjoin(self.test_data_dir, 'gas-carbon-equil.csv'))
def solve(self, solver):
n_points = 12
T = 300
P = 101325
data = np.zeros((n_points, 2 + self.n_species))
phi = np.linspace(0.3, 3.5, n_points)
for i in range(n_points):
X = {self.fuel: phi[i] / self.stoich, 'O2': 1.0, 'N2': 3.76}
self.gas.TPX = T, P, X
mix = ct.Mixture(self.mix_phases)
mix.T = T
mix.P = P
# equilibrate the mixture adiabatically at constant P
mix.equilibrate('HP', solver=solver, max_steps=1000)
data[i, :2] = (phi[i], mix.T)
data[i, 2:] = mix.species_moles
self.compare(data, '../data/gas-carbon-equil.csv')
def Eq(fuel, phi):
gas = ct.Solution('gri30.xml', 'gri30_mix')
gas.set_equivalence_ratio(phi, fuel, air)
mix = ct.Mixture([(gas, 1.0), (carbon, 0.0)])
mix.T = Ti
mix.P = Pi
mix.equilibrate('HP')
print(mix.T)
Xf = 1 - sum(mix.phase(0)['N2', 'O2'].X)
Xff = 1 - sum(mix.phase(0)['N2', 'O2', 'H2O', 'CO2'].X)
Xair = 1 - Xf
dResult = {
'phi': phi,
'Tad': mix.T,
'Xf': Xf,
'Xff': Xff,
'air': Xair,
'O2': mix.phase(0)['O2'].X
}
return dResult
def get_mw(self, conv=ml2l):
""" Initialize parameters for cantera simulation. init() calls this function"""
mx = ct.Mixture(self.phase)
aq = mx.phase_index(self.phase_names[0])
org = mx.phase_index(self.phase_names[1])
mwre = np.zeros(len(self.ree)) # molecular weight of rees
mwslv = np.zeros(len(self.solv)) # mw & densities for 'solvents'
for re in self.ree:
mwre[self.ree.index(re)] = mx.phase(aq).molecular_weights[mx.phase(
aq).species_index(re + '+++')]
for so in self.solv:
if so == 'H2O(L)':
mwslv[self.solv.index(so)] = mx.phase(aq).molecular_weights[
mx.phase(aq).species_index(so)]
else:
mwslv[self.solv.index(so)] = mx.phase(org).molecular_weights[
mx.phase(org).species_index(so)]
return mwre, mwslv
def test_add_species_disabled(self):
ref = ct.Solution('gri30.xml')
reactor = ct.IdealGasReactor(self.phase)
with self.assertRaises(ct.CanteraError):
self.phase.add_species(ref.species('CH4'))
del reactor
gc.collect()
self.phase.add_species(ref.species('CH4'))
flame = ct.FreeFlame(self.phase, width=0.1)
with self.assertRaises(ct.CanteraError):
self.phase.add_species(ref.species('CO'))
del flame
gc.collect()
self.phase.add_species(ref.species('CO'))
mix = ct.Mixture([(self.phase, 2.0)])
with self.assertRaises(ct.CanteraError):
self.phase.add_species(ref.species('CH2O'))
del mix
gc.collect()
self.phase.add_species(ref.species('CH2O'))
'size': 15
},
'tickcolor': 'rgba(0,0,0,0)',
'ticklen': 5,
'showline': True,
'showgrid': True
}
# Setup Cantera
Pi = 101000 # Initial pressure Pa
Ti = 300 # Initial unburned gas temperature K
carbon = ct.Solution('graphite.xml')
# Calls Gas Properties from Gri-MECH
gas = ct.Solution('gri30.xml', 'gri30_mix')
mix = ct.Mixture([(gas, 1.0), (carbon, 0.0)])
fuel10Ah = {'CO2': 44, 'CO': 15, 'H2': 31, 'CH4': 6, 'C3H8': 4}
# 100 Percent Charge C
fuelSom100pct = {'CO2': 30, 'CO': 23, 'H2': 28, 'CH4': 6, 'C2H6': 1, 'C3H8': 4}
# LFP 100 SOC Golubkov 2015 Ethylene binned to Propane
fuelLFP = {
'CO2': 48.3,
'CO': 9.1,
'H2': 29.4,
'CH4': 5.4,
'C2H6': 0.5,
'C3H8': 7.2
}
air = {'N2': 3.76, 'O2': 1}
def setUp(self):
self.mix = ct.Mixture(self.phases)
def setUp(self):
self.mix = ct.Mixture([(self.phase1, 1.0), (self.phase2, 2.0)])
def run(self):
# Gas Mixtures
air_species = self.air # Air
fuel_species = self.fuel
phi = self.phi # Composition
f = self.f
# Temperatures and Pressures
Patm = self.P # Initial Pressure
T = self.T # Initial unburned gas temperature K
P1 = Patm # Initial Pressure
Pa = Patm # Exit pressure outside vent
# Tu = T # Unburned gas temperature
T1 = T # Initial Temperature
# Geometry and Vent
R = self.R # Radius
Cd = self.Cd # Coefficient for vent
Av = self.Av # Vent Area (m2)
S = self.S
# Solution Control
tmax = self.tmax # Max Time for analysis
# Create Gases
carbon = ct.Solution('graphite.xml')
# Calls Gas Properties from Gri-MECH
gas_b = ct.Solution('gri30.xml', 'gri30_mix')
# Calls Gas Properties from Gri-MECH
gas_bv = ct.Solution('gri30.xml', 'gri30_mix')
# Calls Gas Properties from Gri-MECH
gas_u = ct.Solution('gri30.xml', 'gri30_mix')
mix_phases_b = [(gas_b, 1.0), (carbon, 0.0)] # Burned Mixture
mix_phases_u = [(gas_u, 1.0), (carbon, 0.0)] # Unburned Mixture
gas_b.set_equivalence_ratio(phi, fuel_species, air_species)
gas_bv.set_equivalence_ratio(phi, fuel_species, air_species)
gas_u.set_equivalence_ratio(phi, fuel_species, air_species)
gas_b.TP = T, Patm
gas_bv.TP = T, Patm
gas_u.TP = T, Patm
unburned = ct.Mixture(mix_phases_u) # noqa
burned = ct.Mixture(mix_phases_b)
# # Calculate Laminar Flamespeed
# CalcFlamespeed = False
# if CalcFlamespeed:
# # A freely-propagating flat flame
# f = ct.FreeFlame(unburned, width=5)
# # Energy equation enabled
# f.energy_enabled = True
# f.set_max_time_step(1000)
# f.set_refine_criteria(ratio = 2.0, slope = 0.05, curve = 0.05)
# # Solve with multi or mix component transport properties
# f.transport_model = 'Mix'
# f.solve(loglevel=1,auto=True,refine_grid=True)
# S = f.u[0]
# else:
# Xh2 = float(gas_u['H2'].X)
# #Laminar Burning Velocity for Hydrogen
# # From Liu and MacFarlane for Xh2 < 0.42
# A1 = 4.644E-4
# A2 = -2.119E-3
# A3 = 2.344E-3
# A4 = 1.571
# A5 = 3.839E-1
# A6 = -2.21
# xh2O = 0.0 # mol fraction of steam
# S = (((A1 + A2*(0.42-Xh2)+A3*(0.42-Xh2)**2) *
# Tu**(A4+A5*(0.42-Xh2)))*np.exp(A6*xh2O))
# Unburned Gas Properties
cp_aveu = gas_u.cp
cv_aveu = gas_u.cv
W_aveu = gas_u.mean_molecular_weight
rou = gas_u.density
# Burned Gas Properties
# Chemical Equilibrium
# equilibrate the mixture adiabatically at constant P
burned.equilibrate('HP', solver='gibbs', max_steps=1000)
cp_aveb = gas_b.cp # Average Cp
cv_aveb = gas_b.cv # Average Cv
W_aveb = gas_b.mean_molecular_weight # Average Molecular wt
rob = gas_b.density # Average density
Tb = burned.T
gas_bv.equilibrate('UV')
Pf_ = gas_bv.P / Patm
# Ratio of specific heats for unburned gas = Cp/Cvs
gammaU = cp_aveu / cv_aveu
# Ratio of specific heats
gammaB = cp_aveb / cv_aveb
gammaE = (gammaU - 1) / (gammaB - 1)
# gammaE=1.0
# Initial Volume and Mass
V1 = 4.0 / 3.0 * np.pi * R**3 # Initial Volume
mi = rou * V1 # Initial Mass
# print("Unburned Mol Fraction")
# print(gas_u.species_names,'\n', gas_u.X , '\n',
# 'Mass Fraction \n', gas_u.Y)
# print("Burned Mol Fraction")
# print(gas_b.species_names, '\n',gas_b.X ,'\n',
# 'Mass Fraction \n', gas_b.Y)
# print("S: ",S)
# print("Tb: ",Tb)
# print("Pf: ",Pf_)
# print("GammaE:", gammaE)
# print("cp_aveb",cp_aveb)
# start
# initial conditions
P_init = 1
n3init = 1E-5 * (W_aveu / W_aveb) * (Tb / T1)
ninit = 1E-5
init = [P_init, n3init, ninit]
t = np.linspace(0, tmax, 10000)
# Solve ODE's
x = odeint(vent_gas_explosion,
init,
t,
args=(P1, R, V1, gammaE, Pf_, gammaU, mi, gas_u, S, rou,
rob, gammaB, Cd, Av, f, T1, Pa))
# Output
self.P_ = x[:, 0] # Pressure/initial pressure
self.n3 = x[:, 1] # Burnt gas volume
self.n = x[:, 2] # Ratio of burnt mass/initial mass
self.r = R * (self.n3)**(1.0 / 3.0) # Spherical flame radius
self.t = t
self.nu = 1 - self.n # Ratio of unburned mass/initial mass
self.mu = mi * self.nu # Mass of unburned gas
# Number of unburned moles
nmu = self.mu / (gas_u.mean_molecular_weight / 1000)
self.Vu = (1 - self.n3) * V1
self.Tu = self.P_ * Patm * self.Vu / (nmu * RR)
self.gas_u = gas_u
self.gas_b = gas_b
self.gas_bv = gas_bv
self.Tb = Tb
self.Pf_ = Pf_
def areaV(self, Av1):
#Standard Air Composition Attribute
air_species = self.air
#Fuel Gas Composition Passed Into Vent Object on creation
fuel_species = self.fuel
#Equivalence Ratio
phi = self.phi
# Temperatures and Pressures
Patm = self.P # Initial Pressure
T = self.T # Initial unburned gas temperature K
P1 = Patm # Initial Pressure
Pa = Patm # Exit pressure outside vent
# Tu = T # Unburned gas temperature
T1 = T # Initial Temperature
#Geometry parameters
L = self.L
W = self.W
H = self.H
#Face Areas
Aw1 = L * H
Aw2 = W * H
Aw3 = W * L
#Total Surface Area
As = 2 * Aw1 + 2 * Aw2 + Aw3
#Hydraulic Diameter
Dhe = 4 * (Aw2 / (2 * W + 2 * H))
#Area Blockage Ratio
Br = self.Block
#Reduced Pressure
P_red = self.Reduced
Pmax = self.Adiabatic
Po = 0.01325
Pstat = self.Static
#Vent Drag Coefficient
Cd = self.Drag
#Vent Static Activation Pressures
P_stat = self.Static
#Unburned Gas-Air Mixture Sonic Flow Mass Flux(kg/m^2-s)
Gu = 230.1
#Flame speed
Su = self.S
#Cantera Objects
carbon = ct.Solution('graphite.xml')
# Calls Gas Properties from Gri-MECH -- creates burned gas object
gas_b = ct.Solution('gri30.xml', 'gri30_mix')
# Calls Gas Properties from Gri-MECH -- creates unburned object
gas_u = ct.Solution('gri30.xml', 'gri30_mix')
mix_phases_b = [(gas_b, 1.0), (carbon, 0.0)] # Burned Mixture
mix_phases_u = [(gas_u, 1.0), (carbon, 0.0)] # Unburned Mixture
gas_b.set_equivalence_ratio(phi, fuel_species, air_species)
gas_u.set_equivalence_ratio(phi, fuel_species, air_species)
Pi = 101000 #Initial pressure Pa
Ti = 300 #Initital unburned gas temperature K
gas_b.TP = Ti, Pi
gas_u.TP = 300, ct.one_atm
#----------------------
#Unburned gas-air mixture speed of sound (m/s):
#au = self.equilSoundSpeeds(gas_u)[0]
# save properties
rtol = 1.0e-6
maxiter = 8000
gas_u.equilibrate('TP', rtol=rtol, maxiter=maxiter)
s0 = gas_u.s
p0 = gas_u.P
r0 = gas_u.density
# Perturb the pressure
p1 = p0 * 1.0001
# Set the gas to a state with the same entropy and composition but
# The perturbed pressure
gas_u.SP = s0, p1
# Now equilibrate the gas holding S and P constant
gas_u.equilibrate('SP', rtol=rtol, maxiter=maxiter)
ptest = p1 - p0
ztest = gas_u.density - r0
dtest = ptest / ztest
debub = {
'r0': r0,
'density': gas_u.density,
'bottom': ztest,
'top': ptest,
'div': dtest
}
# Equilibrium sound speed
aequil = math.sqrt((p1 - p0) / (gas_u.density - r0))
#print('executed')
au = aequil
#--------
rho_u = gas_b.density
mu_u = gas_b.viscosity
unburned = ct.Mixture(mix_phases_u) # noqa
burned = ct.Mixture(mix_phases_b)
burned.equilibrate('HP', solver='gibbs', max_steps=1000)
gamma_b = gas_b.cp / gas_b.cv
#------------VENT AREA FUNCTION FROM AUSTIN'S SCRIPT-------------------
Dv = math.sqrt((Av1 / self.Number))
#Reynolds number of flame through structure:
Re_flame = rho_u * Su * (0.5 * Dhe) / mu_u
#Phi 1: Based on Reynolds Number of Flame Front:
phi_1 = max(1, (Re_flame / 4000)**0.39)
#Maximum Velocity through Vent (m/s):
uv = min(math.sqrt(P_red * 2 * 10**5 / rho_u), au)
#Reynolds number through vent
Re_vent = 0.5 * rho_u * uv * Dv / mu_u
#Phi 2: Based on Reynolds Number through Vent:
beta1 = 1.23
beta2 = 2.37 * 10**-3
phi_2 = max(1, beta1 * (Re_vent / 10**6)**((beta2 / Su)**0.5))
#Lambda 0:
Lambda_0 = phi_1 * phi_2
#Lambda 1 Based on Obstructed surface area (m^2):
Aobs = 0.3 * As
#Obstruction Correction Factor
if Aobs < 0.2 * As:
Lambda_1 = Lambda_0
elif Aobs >= 0.2 * As:
Lambda_1 = Lambda_0 * math.exp(math.sqrt((Aobs / As) - 0.2))
#L/D
L_D = L / Dhe
#Solving for Lambda:
if L_D < 2.5:
Lambda = Lambda_1
elif L_D >= 2.5:
Lambda = Lambda_1 * (1 + ((L_D / 2.5) - 1)**2)
# #L/D Correction Factor
# if L_D > 5:
# print ("L/D Above 5 see NFPA 68 Chapter 9")
# elif Pmax > 10:
# print ("Pmax Above 10 bar-g see NFPA 68")
#Solving for vent size:
C = (0.5 * Su * rho_u * Lambda /
(Gu * Cd)) * (((Pmax + 1) /
(Po + 1))**(1 / gamma_b) - 1) * (Po + 1)**0.5
delta = (((Pstat + 1) / (Po + 1))**(1 / gamma_b) - 1) / ((
(Pmax + 1) / (Po + 1))**(1 / gamma_b) - 1)
#Pred Corrction Factor
if P_red <= 0.5:
Avo = As * C / math.sqrt(P_red)
elif P_red > 0.5:
Avo = (As * Su * rho_u * Lambda /
(Gu * Cd)) * (1 - ((P_red + 1) /
(Pmax + 1))**(1 / gamma_b)) / (
((P_red + 1) /
(Pmax + 1))**(1 / gamma_b) - delta)
return (Avo)
#Unburned gas-air mixture speed of sound (m/s):
au = equilSoundSpeeds(gas)[0]
#Burned Mixture
Pi = 101000 #Initial pressure Pa
Ti = 300 #Initial unburned gas temperature K
gas_b.TP = Ti, Pi
#Mass Density of Unburned Gas-Air Mixture (kg/m^3):
rho_u = gas_b.density
#Unburned gas-air mixture dynamic viscosity (kg/m-s):
mu_u = gas_b.viscosity
#Suppress the next two lines for unburned data
burned = ct.Mixture(mix_phases_b)
#Equilibrate the mixture adiabatically at constant P
burned.equilibrate('HP', solver='gibbs', max_steps=1000)
gamma_b = gas_b.cp / gas_b.cv #Suppress for unburned data
#Structure Surface Area (m^2):
#Length (m):
L = 24.4
#Depth (m):
D = 30.5
#Height (m):
H = 6.1
def set_in_moles(self, feed_vol):
"""Function that initializes mole fractions to input feed_vol
This function is called at initialization
Sets in_moles to a pd.DataFrame containing initial mole fractions
Columns for species and rows for different experiments
This function also calls update_predicted_dict
:param feed_vol: (float) feed volume of mixture (L)
"""
phases_copy = self._phases.copy()
exp_df = self._exp_df.copy()
solvent_name = self._aq_solvent_name
extractant_name = self._extractant_name
diluant_name = self._diluant_name
solvent_rho = self._aq_solvent_rho
extractant_rho = self._extractant_rho
diluant_rho = self._diluant_rho
extracted_species_names = self._extracted_species_ion_names
extracted_species_list = self._extracted_species_list
mixed = ct.Mixture(phases_copy)
aq_ind = None
solvent_ind = None
for ind, phase in enumerate(phases_copy):
if solvent_name in phase.species_names:
aq_ind = ind
solvent_ind = phase.species_names.index(solvent_name)
if aq_ind is None:
raise Exception('Solvent "{0}" not found \
in xml file'.format(solvent_name))
if aq_ind == 0:
org_ind = 1
else:
org_ind = 0
self._aq_ind = aq_ind
self._org_ind = org_ind
extractant_ind = phases_copy[org_ind].species_names.index(
extractant_name)
diluant_ind = phases_copy[org_ind].species_names.index(diluant_name)
extracted_species_ind_list = [
phases_copy[aq_ind].species_names.index(extracted_species_name)
for extracted_species_name in extracted_species_names
]
extracted_species_charges = np.array([
phases_copy[aq_ind].species(extracted_species_ind).charge
for extracted_species_ind in extracted_species_ind_list
])
self._extracted_species_charges = extracted_species_charges
mix_aq = mixed.phase(aq_ind)
mix_org = mixed.phase(org_ind)
solvent_mw = mix_aq.molecular_weights[solvent_ind] # g/mol
extractant_mw = mix_org.molecular_weights[extractant_ind]
diluant_mw = mix_org.molecular_weights[diluant_ind]
if solvent_rho is None:
solvent_rho = mix_aq(aq_ind).partial_molar_volumes[
solvent_ind] / solvent_mw * 1e6 # g/L
self._aq_solvent_rho = solvent_rho
if extractant_rho is None:
extractant_rho = mix_org(org_ind).partial_molar_volumes[
extractant_ind] / extractant_mw * 1e6
self._extractant_rho = extractant_rho
if diluant_rho is None:
diluant_rho = mix_org(org_ind).partial_molar_volumes[
extractant_ind] / extractant_mw * 1e6
self._diluant_rho = diluant_rho
in_moles_data = []
aq_phase_solvent_moles = feed_vol * solvent_rho / solvent_mw
for index, row in exp_df.iterrows():
h_plus_moles = feed_vol * row['h_i']
hydroxide_ions = 0
extracted_species_moles = np.array([
feed_vol * row['{0}_aq_i'.format(extracted_species)]
for extracted_species in extracted_species_list
])
extracted_species_charge_sum = np.sum(extracted_species_charges *
extracted_species_moles)
chlorine_moles = extracted_species_charge_sum + h_plus_moles
extractant_moles = feed_vol * row['z_i']
extractant_vol = extractant_moles * extractant_mw / extractant_rho
diluant_vol = feed_vol - extractant_vol
diluant_moles = diluant_vol * diluant_rho / diluant_mw
complex_moles = np.zeros(len(extracted_species_list))
species_moles_aq = [
aq_phase_solvent_moles, h_plus_moles, hydroxide_ions,
chlorine_moles
]
species_moles_aq.extend(list(extracted_species_moles))
species_moles_aq.append(self.nacl_molarity * feed_vol)
species_moles_aq[3] += self.nacl_molarity * feed_vol
species_moles_org = [extractant_moles, diluant_moles]
species_moles_org.extend(list(complex_moles))
if aq_ind == 0:
species_moles = species_moles_aq + species_moles_org
else:
species_moles = species_moles_org + species_moles_aq
in_moles_data.append(species_moles)
self._in_moles = pd.DataFrame(in_moles_data,
columns=mixed.species_names)
self.update_predicted_dict()
return None
def test_invalid_phase_type(self):
water = ct.Water()
with self.assertRaisesRegex(ct.CanteraError, 'not compatible'):
self.mix = ct.Mixture([(self.phase1, 1.0), (water, 2.0)])
"""
import cantera as ct
import csv
# create objects representing the gas phase and the condensed phases. The gas
# is a mixture of multiple species, and the condensed phases are all modeled
# as incompressible stoichiometric substances. See file KOH.yaml for more
# information.
phases = ct.import_phases('KOH.yaml', [
'K_solid', 'K_liquid', 'KOH_a', 'KOH_b', 'KOH_liquid', 'K2O2_solid',
'K2O_solid', 'KO2_solid', 'ice', 'liquid_water', 'KOH_plasma'
])
# create the Mixture object from the list of phases
mix = ct.Mixture(phases)
equil_data = []
# loop over temperature
for n in range(100):
t = 350.0 + 50.0 * n
print('T = {0}'.format(t))
mix.T = t
mix.P = ct.one_atm
mix.species_moles = "K:1.03, H2:2.12, O2:0.9"
# set the mixture to a state of chemical equilibrium holding
# temperature and pressure fixed
# mix.equilibrate("TP",maxsteps=10000,loglevel=1)
mix.equilibrate("TP", max_steps=10000, log_level=0)
def test_invalid_phase_type(self):
water = ct.Water()
with self.assertRaises(ct.CanteraError):
self.mix = ct.Mixture([(self.phase1, 1.0), (water, 2.0)])
'''
import cantera as ct
mix = ct.Solution('liquidvapor.cti')
#initial_temp,initial_press =[float(val) for val in input().split()]
mix.TPX = 300,ct.one_atm,'H2O:1'
mix.equilibrate('HP')
print(mix.P_sat/ct.one_atm)
'''
import cantera as ct
liquid = ct.Solution('water.cti', 'liquid_water')
solid = ct.Solution('water.cti', 'ice')
gas = ct.Solution('h2o2.cti')
for T in [280, 400]:
gas.TPX = 300, 101325, 'AR:1.0, H2O:0.0'
mix = ct.Mixture([(gas, 0.01), (liquid, 0.99), (solid, 0.0)])
mix.T = T
mix.P = 101325
mix.equilibrate('TV', solver='gibbs')
print(gas['H2O'].X * mix.P)
print('T = {}'.format(T))
#mix()
import numpy as np
#==============================================================================
# set parameters
#==============================================================================
To = 298.195 # K (reference temperature)
R = ct.gas_constant # 8314.47215 Pa*m^3/K/kmol
#==============================================================================
# load components to phases
#==============================================================================
s = ct.Solution('data/min-species.xml','solid')
g = ct.Solution('data/min-species.xml','gas')
#print s.species_names
air = ct.Solution('data/air.cti','air')
f = ct.Mixture([(s,1),(g,1)])
# preallocate variable
nsp = f.n_species
#==============================================================================
# get standard state properties
#==============================================================================
# molecular weight
Mw_s = s.molecular_weights
Mw_g = g.molecular_weights
Mw = np.concatenate((Mw_s, Mw_g))
# standard enthalpy of formation
Hfo_s = s.standard_enthalpies_RT*To*R
Hfo_g = g.standard_enthalpies_RT*To*R
Hfo = np.concatenate((Hfo_s, Hfo_g))
## find important indices
def __init__(self,
config_file,
prep_capex=0,
prep_opex=0,
prep_revenue=0,
prep_npv=0):
"""Constructor.
"""
self.confDict = utilities.read_config(config_file)
solventxHome = self.confDict["solventxHome"]
reeComps = self.confDict['compositions']
self.xmlData = self.confDict['xmlData']
self.modulesData = self.confDict['modules']
self.xml = os.path.join(
solventxHome, self.xmlData['xml'], self.xmlData['phase'] + '_' +
''.join(self.modulesData["input"]) + '.xml')
# Set required data
self.phase_names = self.confDict["phasenames"] # from xml input file
self.phase = ct.import_phases(self.xml, self.phase_names)
# Derived and/or reusable system parameters
self.column = self.coltypes # Column name
self.solv = self.confDict[
"solvents"] # solvent list -.i.e., electrolyte, extractant and organic diluent
# ree by modules
self.ree = self.modulesData[
"input"] #self.REEs[self.moduleID] # (rare earth) metal list
# Cantera indices
self.mix = ct.Mixture(self.phase)
self.aq = self.mix.phase_index(self.phase_names[0])
self.org = self.mix.phase_index(self.phase_names[1])
self.ns = self.mix.n_species
self.naq = self.mix.phase(self.aq).n_species
self.norg = self.mix.phase(self.org).n_species
self.HA_Index = self.mix.species_index(
self.org,
'(HA)2(org)') # index of extractant in canera species list
self.Hp_Index = self.mix.species_index(
self.aq, 'H+') # index of H+ in cantera species list
self.Cl_Index = self.mix.species_index(
self.aq, 'Cl-') # index of Cl in cantera species list
self.canteranames = self.mix.species_names
self.fixed_species = ['H2O(L)', 'OH-', 'Cl-', 'dodecane']
self.canteravars = [
ij for ij in self.canteranames if ij not in self.fixed_species
] # 'Cl-',
self.nsy = len(self.canteravars)
self.naqy = len([
ij for ij in self.mix.species_names[:self.naq]
if ij not in self.fixed_species
])
self.norgy = len([
ij for ij in self.mix.species_names[self.naq:]
if ij not in self.fixed_species
])
self.mwre,\
self.mwslv = self.get_mw() # g/mol
self.rhoslv = [1000, 960, 750] # [g/L]
self.upper = [reeComps[i]['upper'] for i in self.ree]
self.lower = [reeComps[i]['lower'] for i in self.ree]
ree_mass = [
np.random.uniform(i, j) for i, j in zip(self.lower, self.upper)
]
self.get_conc(ree_mass)
self.purity_spec = .99 # not needed?
self.recov_spec = .99 # not needed?
self.revenue = [0, 0, 0]
self.Ns = [0, 0, 0]
self.nsp = pd.DataFrame() # feed streams (aq and org) for each column
self.nsp0 = pd.DataFrame() # feed streams (aq and org) for each column
self.y = {} # all compositions
self.Ns = {}
# phases
# complete_species = [species[S] for S in ('CH4','O2','N2','CO2','H2O')]
# gas = ct.Solution(thermo='IdealGas', species=complete_species)
gas = ct.Solution('r_creck_52.cti')
carbon = ct.Solution('graphite.xml')
# the phases that will be included in the calculation, and their initial moles
mix_phases = [(gas, 1.0), (carbon, 0.0)]
# gaseous fuel species
fuel_species = 'CH4'
##############################################################################
mix = ct.Mixture(mix_phases)
# create some arrays to hold the data
phi = 0.7
# find fuel, nitrogen, and oxygen indices
ifuel = gas.species_index(fuel_species)
io2 = gas.species_index('O2')
in2 = gas.species_index('N2')
stoich_O2 = gas.n_atoms(fuel_species,
'C') + 0.25 * gas.n_atoms(fuel_species, 'H')
X = np.zeros(gas.n_species)
X[ifuel] = phi
X[io2] = stoich_O2
def test_invalid_phase_type(self):
water = ct.Water()
with self.assertRaises(Exception):
self.mix = ct.Mixture([(self.phase1, 1.0), (water, 2.0)])