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@yoelcortes
yoelcortes committed May 24, 2024
2 parents 6f178bc + 33f806a commit b3ef170
Showing 1 changed file with 152 additions and 30 deletions.
182 changes: 152 additions & 30 deletions biosteam/units/design_tools/aeration.py
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Original file line number Diff line number Diff line change
Expand Up @@ -97,34 +97,6 @@ def C_O2_L(T, P_O2): # Commonly used, so here for convinience
partial pressure of O2 in the gas [bar]."""
return P_O2 * Henrys_law_constant(T, *H_coefficients['O2'])

def log_mean_driving_force(C_sat_out, C_sat_in, C_out, C_in=None):
"""
Return the driving force for mass transfer. In small vessels (<1 m tall)
where both liquid concentration and saturation are almost constant, the simple
form is adequate [11]_. In tall vessels, the log-mean driving force should be
used for more accuracy, since both the local concentration and the saturation
concentration are different in the top and bottom of a bioreactor [11]_.
Parameters
----------
C_sat_out : float
Saturated concentration entering the bioreactor.
C_sat_out : float
Saturated concentration exiting the bioreactor.
C_out : float, optional
Outlet concentration.
C_in : float
Inlet concentration. Defaults to the outlet concentration, which
assumes perfect mixing and oxygen uptake rate is the same everywhere.
"""
if C_in is None: C_in = C_out # Assume perfect mixing and oxygen uptake rate is the same everywhere.
dC_out = C_sat_out - C_out
dC_in = C_sat_in - C_in
if dC_out < 1e-9: # This is not theoretically possible, but may be an assumption
dC_out = 1e-9 # Assume it near zero
return (dC_out - dC_in) / log(dC_out / dC_in)

kLa_methods = {}
kLa_method_names = {
'Bubble column': [],
Expand Down Expand Up @@ -183,7 +155,7 @@ def kLa_stirred_Riet(P, V, U, coefficients=None):
# bubble column reactors.
# Take present that the units of the efficiency factor are [m**-1].
# This values are
# - 0.016-0.028 m^-1 for coarse bubble diffusers
# - 0.016-0.028 m**-1 for coarse bubble diffusers
# - 0.07-0.1 m^-1 for fine bubble diffusers
# """
# K = None
Expand Down Expand Up @@ -421,7 +393,36 @@ def kla_bubcol_Suh(D, mu_l, rho_l, D_l, g, sigma_l, epsilon_g, V_g, V_l, coeffic
Air-Aqueous Sucrose Solution
"""

kla = (D_l/(D**2)) * 0.018 * (mu_l/(rho_l * D_l))**(0.5) * ((g*rho_l*D**2)/sigma_l)**(0.75) * (g*D**3*rho_l**2/(mu_l**2))**(0.39)*(V_g/(sqrt(g*D)))
kla = (D_l/(D**2)) * 0.018 * (mu_l/(rho_l * D_l))**(0.5) * ((g*rho_l*D**2)/sigma_l)**(0.75) * (g*D**3*rho_l**2/(mu_l**2))**(0.39)*(V_g/(sqrt(g*D)))**0.51
return kla
@register
def kla_bubcol_Dewes(V_g, mu_l, rho_g):
"""
Returns the KLa coefficient for a bubble column reactor based on the Dewes & Schumpe (1997) correlation.
-------
Parameters:
V_g: float
Superficial gas velocity, [m/s]
mu_l: float
Viscosity of the liquid, [mPa.s]
rho_g: float
Density of the gas, [kg/m^3]
-------
References:
Dewes, I., & Schumpe, A. (1997).
Gas density effect on mass transfer in the slurry bubble column.
Chemical Engineering Science, 52(21–22), 4105–4109. https://doi.org/10.1016/S0009-2509(97)00252-2
-------
Notes:
This correlation is valid under the following range of values:
D_c: 0.115 m -> Diameter of the column [m]
H_l: 1.37 m -> Liquid height in the column [m]
V_g: 0.01 - 0.08 m/s -> Superficial gas velocity [m/s]
mu_l: 1.35 - 583 mPa.s -> Viscosity of the liquid [mPa.s]
rho_g: 0.4 - 18.8 kg/m^3 -> Density of the gas [kg/m^3]
"""

kla = V_g**0.90 * mu_l**(-0.55) * rho_g**0.46
return kla

@register
Expand Down Expand Up @@ -578,3 +579,124 @@ def P_at_kLa_Riet(kLa, V, U, coefficients=None):
else:
a, b, c = coefficients
return (kLa / (a * U ** c)) ** (1 / b) * V

def log_mean_driving_force(C_sat_out, C_sat_in, C_out, C_in=None):
"""
Return the driving force for mass transfer. In small vessels (<1 m tall)
where both liquid concentration and saturation are almost constant, the simple
form is adequate [11]_. In tall vessels, the log-mean driving force should be
used for more accuracy, since both the local concentration and the saturation
concentration are different in the top and bottom of a bioreactor [11]_.
Parameters
----------
C_sat_out : float
Saturated concentration entering the bioreactor.
C_sat_out : float
Saturated concentration exiting the bioreactor.
C_out : float, optional
Outlet concentration.
C_in : float
Inlet concentration. Defaults to the outlet concentration, which
assumes perfect mixing and oxygen uptake rate is the same everywhere.
"""
if C_in is None: C_in = C_out # Assume perfect mixing and oxygen uptake rate is the same everywhere.
dC_out = C_sat_out - C_out
dC_in = C_sat_in - C_in
if dC_out < 1e-9: # This is not theoretically possible, but may be an assumption
dC_out = 1e-9 # Assume it near zero
return (dC_out - dC_in) / log(dC_out / dC_in)

if __name__ == "__main__":
print('hola')

repeated_names = [
('U_g', ('U_G', 'V_G')),

]
fermentation_variables_bub_col = {
'Dashpande': {
'epsilon_g': (0.5, 1.2),
'K': (0.016, 0.028), # for coarse bubble diffusers 'K': (0.07, 0.1), # for fine bubble diffusers
'M_l': 0.018, # kg/mol
'Rhat': 8.314, # J/mol-K
'T': 298.15, # K
'rho_l': 1000, # kg/m^3
'U_g': (0.01,0.1), # m/s
},
'DeJesus': {
'Q':(0, 1.6), # vvm
'mu': (0.001, 0.1), # Pa.s
'k': (0.1, 100), # Pa.s^n
'n': (0, 2) # Flow behavior index <1 for pseudoplastic, >1 for dilatant, 1 for Newtonian
},
'Akita_Yoshida': {
'D': 0.15, # m
'H': 4, # m
'V_g': (0, 0.33), # m/s
'mu_l': (0.5, 100), # Cp 1 water, 100 xanthan
'rho_l': (995, 1043), # kg/m^3
'D_l': (1.68 * 10**-9, 3.24 * 10**-9) , # m^2/s
'g': 9.81, # m/s^2
'sigma_l': (0.0348,0.0728), # N/m
'epsilon_g': (0.01, 1) # m/s
},
'Posarac_Tekic': {
'D': 0.1, # m
'H': 2.5, # m
'V_g': (0.008, 0.08), # m/s
'mu_l': (0.5, 100), # Cp 1 water, 100 xanthan
'rho_l': (995, 1043), # kg/m^3
'D_l': (1.68 * 10**-9, 3.24 * 10**-9), # m^2/s
'sigma_l': (0.0348,0.0728), # N/m
'epsilon_g': (0.01, 1) # m/s
},
'Seno': {
'D': 0.0464, # m
'H': 1.36, # m
'V_g': (0.005, 0.04), # m/s
'V_l': (0.005, 0.1), # m/s
'rho_l': (995, 1043), # kg/m^3
'mu_l': (0.653, 1.31), # Cp 1 water, 100 xanthan
'D_l': (1.68 * 10**-9, 3.24 * 10**-9), # m^2/s
'g': 9.81, # m/s^2
'sigma_l': (0.0348,0.0728), # N/m
'epsilon_g': (0.01, 1) # m/s
},
'Suh': {
'D': 0.15, # m
'H': 2.9, # m
'V_g': (0.005, 0.04), # m/s
'rho_l': (1001, 1264), # kg/m^3
'mu_l': (0.653, 1.31), # Cp 1 water, 100 xanthan
'D_l': (0.318 * 10**-9, 2.5 * 10**-9) , # m^2/s
'g': 9.81, # m/s^2
'sigma_l': (0.0656,0.0746), # N/m
'epsilon_g': (0.01, 1) # m/s
},
'Shah': {
'D': 0.29, # m
'H': 0.2, # m
'V_g': (0.021, 0.105), # m/s
'V_l': (0.0005, 0.002), # m/s
'rho_l': (1, 50), # kg/m^3
'mu_l': (1, 50), # Cp 1 water, 100 xanthan
},
}

fermentation_variables_stirred = {
'Labik':{
'N': (4.17, 14.17), # s^-1
'D':(0.1, 0.2), # m
'v_s': (2.12 * 1e-3, 8.48 * 1e-3) , # m/s
'P0': (100, 10000),
},
'Galaction':{ # look into what is better for the P_a/V and P/V
'P_a/V' : (30,120), # W/m^3
'v_s': (0.8 * 1e-3, 5 * 1e-3), # m/s
'C_x': (5, 150), # g/l dry weight
'P/V': (10, 1900), # W/m^3

}
}

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