def calculo(self):
ind1 = self.Comp1.currentIndex()
ind2 = self.Comp2.currentIndex()
if ind1 != ind2:
zi = arange(0.025, 1., 0.025)
id1 = self.indices[ind1]
id2 = self.indices[ind2]
x = [0]
y = [0]
for z in zi:
try:
fraccion = [0.] * len(self.indices)
fraccion[ind1] = z
fraccion[ind2] = 1 - z
mez = Mezcla(tipo=3,
fraccionMolar=fraccion,
caudalMasico=1.)
tb = mez.componente[0].Tb
corr = Corriente(T=tb, P=101325., mezcla=mez)
T = corr.eos._Dew_T()
corr = Corriente(T=T, P=101325., mezcla=mez)
while corr.Liquido.fraccion[0] == corr.Gas.fraccion[
0] and corr.T < corr.mezcla.componente[1].Tb:
corr = Corriente(T=corr.T - 0.1, P=101325., mezcla=mez)
x.append(corr.Liquido.fraccion[0])
y.append(corr.Gas.fraccion[0])
except:
pass
x.append(1)
y.append(1)
self.rellenar(x, y)
a7, b7 = 0.0705233, -0.044448
a8, b8 = 0.504087, 1.32245
a9, b9 = 0.0307452, 0.179433
a10, b10 = 0.0732828, 0.463492
a11, b11 = 0.006450, -0.022143
Bo = (a1 + b1 * cmp.f_acent) * cmp.Vc
Ao = (a2 + b2 * cmp.f_acent) * R_atml * cmp.Tc * cmp.Vc
Co = (a3 + b3 * cmp.f_acent) * R_atml * cmp.Tc**3 * cmp.Vc
gamma = (a4 + b4 * cmp.f_acent) * (cmp.Vc)**2
b = (a5 + b5 * cmp.f_acent) * (cmp.Vc)**2
a = (a6 + b6 * cmp.f_acent) * R_atml * cmp.Tc * (cmp.Vc)**2
alfa = (a7 + b7 * cmp.f_acent) * (cmp.Vc)**3
c = (a8 + b8 * cmp.f_acent) * R_atml * cmp.Tc**3 * (cmp.Vc)**2
Do = (a9 + b9 * cmp.f_acent) * R_atml * cmp.Tc**4 * cmp.Vc
d = (a10 + b10 * cmp.f_acent) * R_atml * cmp.Tc**2 * (cmp.Vc)**2
Eo = (a11 + b11 * cmp.f_acent *
exp(-3.8 * cmp.f_acent)) * R_atml * cmp.Tc**5 * cmp.Vc
return Ao, Bo, Co, Do, Eo, a, b, c, d, alfa, gamma
_all = [BWRS]
if __name__ == "__main__":
from lib.mezcla import Mezcla
mezcla = Mezcla(2,
ids=[10, 38, 22, 61],
caudalUnitarioMolar=[0.3, 0.5, 0.05, 0.15])
eq = BWRS(340, 101325, mezcla)
print(eq.x)
__doi__ = {
"autor": "Twu, C.H., Coon, J.E., Cunningham, J.R.",
"title": "A New Generalized Alpha Function for a Cubic Equation of "
"State Part 1. Peng-Robinson equation",
"ref": "Fluid Phase Equilibria 105 (1995) 49-59",
"doi": "10.1016/0378-3812(94)02601-v"
},
OmegaA = 0.457235528921
OmegaB = 0.0777960739039
def _alfa(self, cmp, T):
Tr = T / cmp.Tc
alpha0 = Tr**(-0.171813) * exp(0.125283 * (1 - Tr**1.77634)) # Eq 11
alpha1 = Tr**(-0.607352) * exp(0.511614 * (1 - Tr**2.20517)) # Eq 12
# Eq 9
alpha = alpha0 + cmp.f_acent * (alpha1 - alpha0)
return 0, alpha
if __name__ == "__main__":
from lib.mezcla import Mezcla
mix = Mezcla(5, ids=[4], caudalMolar=1, fraccionMolar=[1])
eq = PRTwu(300, 9.9742e5, mix)
print('%0.0f %0.1f' % (eq.Vg.ccmol, eq.Vl.ccmol))
eq = PRTwu(300, 42.477e5, mix)
print('%0.1f' % (eq.Vl.ccmol))
# f_acent = (0.01100, 0.02200, -0.00200)
# x = (0.50000, 0.30000, 0.20000)
from lib.mezcla import Mezcla
from lib.compuestos import Componente
ch4 = Componente(2)
ch4.Tc, ch4.Pc, ch4.f_acent = 190.564, 4599200, 0.011
o2 = Componente(47)
o2.Tc, o2.Pc, o2.f_acent = 154.581, 5042800, 0.022
ar = Componente(98)
ar.Tc, ar.Pc, ar.f_acent = 150.687, 4863000, -0.002
mix = Mezcla(5,
customCmp=[ch4, o2, ar],
caudalMolar=1,
fraccionMolar=[0.5, 0.3, 0.2])
print(2222)
eq = PRMathiasCopeman(800, 34933409.8798343, mix)
print(eq._phir(800, 5000, eq.yi))
from lib.mezcla import Mezcla
from lib.compuestos import Componente
ch4 = Componente(2)
ch4.Tc, ch4.Pc, ch4.f_acent = 190.564, 4599200, 0.011
o2 = Componente(47)
o2.Tc, o2.Pc, o2.f_acent = 154.581, 5042800, 0.022
ar = Componente(98)
ar.Tc, ar.Pc, ar.f_acent = 150.687, 4863000, -0.002
mix = Mezcla(5,
customCmp=[ch4, o2, ar],
# mix = Mezcla(5, ids=[46, 2], caudalMolar=1, fraccionMolar=[0.2152, 0.7848])
# eq = SRK(144.26, 2.0684e6, mix)
# print(eq.rhoL.kmolm3)
# # Ejemplo 6.6, Wallas, pag 340
# mezcla = Mezcla(2, ids=[1, 2, 40, 41], caudalUnitarioMolar=[0.3177, 0.5894, 0.0715, 0.0214])
# P = unidades.Pressure(500, "psi")
# T = unidades.Temperature(120, "F")
# eq = SRK(T, P, mezcla)
# print(T)
# print(eq.x)
# print([x*(1-eq.x)*5597 for x in eq.xi])
# print([y*eq.x*5597 for y in eq.yi])
# print(eq.Ki)
# Example 6.6 wallas
P = unidades.Pressure(20, "atm")
mix = Mezcla(5, ids=[23, 5], caudalMolar=1, fraccionMolar=[0.607, 0.393])
eq1 = SRK(300, P, mix)
eq2 = SRK(400, P, mix)
print(eq1._Dew_T(P))
print(eq2._Dew_T(P))
# eq = SRK(500, P, mezcla)
# print(eq._Dew_T(P))
kw["a"] = self.tita
kw["dat"] = damt
kw["datt"] = damtt
kw["dattt"] = damttt
print(tau, delta, kw)
p = CubicHelmholtz(tau, delta, **kw)
p["tau"] = tau
p["delta"] = delta
print("fir: ", p["fir"])
print("fird: ", p["fird"] * delta)
print("firt: ", p["firt"] * tau)
print("firdd: ", p["firdd"] * delta**2)
print("firdt: ", p["firdt"] * delta * tau)
print("firtt: ", p["firtt"] * tau**2)
print("firddd: ", p["firddd"] * delta**3)
print("firddt: ", p["firddt"] * delta**2 * tau)
print("firdtt: ", p["firdtt"] * delta * tau**2)
print("firttt: ", p["firttt"] * tau**3)
print("P", (1 + delta * p["fird"]) * R * self.T * self.rho - self.P)
self.fir = p
if __name__ == "__main__":
from lib.mezcla import Mezcla
mix = Mezcla(tipo=5,
caudalMolar=1,
ids=[2, 47, 98],
fraccionMolar=[0.5, 0.3, 0.2])
eq = PRMathiasCopeman(800, 34937532, mix)
self.Bi = [bi*self.P/R/self.T for bi in self.bi]
self.Ai = [ai*self.P/(R*self.T)**2 for ai in self.ai]
def _lib(self, cmp, T):
a0 = 0.42747*R**2*cmp.Tc**2/cmp.Pc
alfa = (self.T/cmp.Tc)**-0.5
b = 0.08664*R*cmp.Tc/cmp.Pc
return a0*alfa, b
def _GEOS(self, xi):
am, bm = self._mixture("RK", xi, [self.ai, self.bi])
delta = bm
epsilon = 0
return am, bm, delta, epsilon
if __name__ == "__main__":
from lib.mezcla import Mezcla
from lib import unidades
# mix = Mezcla(2, ids=[10, 38, 22, 61],
# caudalUnitarioMolar=[0.3, 0.5, 0.05, 0.15])
# eq = RK(340, 101325, mix)
mezcla = Mezcla(2, ids=[1, 2, 40, 41],
caudalUnitarioMolar=[0.31767, 0.58942, 0.07147, 0.02144])
P = unidades.Pressure(485, "psi")
T = unidades.Temperature(100, "F")
eq = RK(T, P, mezcla, flory=1)
# Eq 21
bptr = 1 - 0.1519*cmp.f_acent - 3.9462*cmp.f_acent**2 + \
7.0539*cmp.f_acent**3
bpt = bptr * bc
mb = bptr - 1 # Eq 17
apt = 29.7056 * bpt * R * Tpt # Eq 19
b = bc * (1 + mb * (1 - Tita)) # Eq 16
ma = (apt / ac)**0.5 - 1 # Eq 11
a = ac * (1 + ma * (1 - Tita**0.5))**2 # Eq 10
return a, b
if __name__ == "__main__":
from lib.mezcla import Mezcla
mix = Mezcla(5, ids=[4], caudalMolar=1, fraccionMolar=[1])
eq = Nasrifar(300, 9.9742e5, mix)
print('%0.1f' % (eq.Vl.ccmol))
eq = Nasrifar(300, 42.477e5, mix)
print('%0.1f' % (eq.Vg.ccmol))
mix = Mezcla(5,
ids=[46, 2],
caudalMolar=1,
fraccionMolar=[0.04752, 0.95248])
eq = Nasrifar(105, 5e7, mix)
print(eq.rhoL.kmolm3)