def as_thermo(thermo, chemicals):
try:
thermo = settings.get_default_thermo(thermo)
except:
thermo = tmo.Thermo(chemicals)
else:
thermo = tmo.Thermo(chemicals,
Gamma=thermo.Gamma,
Phi=thermo.Phi,
PCF=thermo.PCF)
return thermo
def test_reaction():
# Test corners in code
tmo.settings.set_thermo(['H2O', 'H2', 'O2'], cache=True)
reaction = tmo.Reaction('', reactant='H2O', X=1.,
correct_atomic_balance=True)
assert not reaction.stoichiometry.any()
# Test math cycles, making sure they balance out
reaction = tmo.Reaction('2H2O -> 2H2 + O2', reactant='H2O',
correct_atomic_balance=True, X=0.5)
same_reaction = reaction.copy()
reaction += same_reaction
reaction -= same_reaction
assert_allclose(reaction.X, same_reaction.X)
reaction *= 2.
reaction /= 2.
assert_allclose(reaction.X, same_reaction.X)
# Test negative math
negative_reaction = 2 * -reaction
assert_allclose(negative_reaction.X, -1.)
# Test errors with incompatible phases
reaction = tmo.Reaction('H2O,l -> H2,g + O2,g', reactant='H2O',
correct_atomic_balance=True, X=0.7)
stream = tmo.MultiStream(None, l=[('H2O', 10)], phases='lL')
with pytest.raises(ValueError): reaction(stream)
# Test errors with incompatible chemicals
stream = tmo.MultiStream(None, l=[('Water', 10)],
thermo=tmo.Thermo(['Water', 'Ethanol']),
phases='gl')
with pytest.raises(tmo.exceptions.UndefinedChemical): reaction(stream)
def set_thermo(self, thermo, cache=None):
"""
Set the default Thermo object. If `thermo` is not a Thermo object,
an attempt is made to convert it to one.
Parameters
----------
thermo : Thermo or Iterable[Chemical or str]
A Thermo object or iterable of chemicals or chemical IDs.
cache : bool, optional
Wether or not to use cached chemicals.
"""
if not isinstance(thermo, tmo.Thermo):
thermo = tmo.Thermo(thermo, cache=cache)
self._thermo = thermo
def set_thermo(self, thermo, cache=None, skip_checks=False):
"""
Set the default Thermo object. If `thermo` is not a Thermo object,
an attempt is made to convert it to one.
Parameters
----------
thermo : Thermo or Iterable[Chemical or str]
A Thermo object or iterable of chemicals or chemical IDs.
cache : bool, optional
Wether or not to use cached chemicals.
skip_checks : bool, optional
Whether to skip checks for missing or invalid properties.
"""
if not isinstance(thermo, (tmo.Thermo, tmo.IdealThermo)):
thermo = tmo.Thermo(thermo, cache=cache, skip_checks=skip_checks)
self._thermo = thermo
# %% Facilities
# tmo.Stream.default_ID_number = 500
J7_1 = bst.Junction('J7_1', upstream=S402 - 0, downstream=Stream())
BT = bst.facilities.BoilerTurbogenerator('BT',
ins=(J7_1 - 0),
turbogenerator_efficiency=0.85)
BT.outs[-1].T = 373.15
# tmo.Stream.default_ID_number = 700
CWP = bst.facilities.ChilledWaterPackage('CWP')
CT = bst.facilities.CoolingTower('CT')
CT.outs[1].T = 273.15 + 28
water_thermo = tmo.Thermo(tmo.Chemicals(['Water']))
process_water = tmo.Stream(ID='process_water', thermo=water_thermo)
process_water_streams = (caustic, stripping_water, process_water1,
process_water2, steam, BT - 1, CT - 1)
def update_water_loss():
process_water.imol['Water'] = sum(
[i.imol['Water'] for i in process_water_streams])
makeup_water = Stream('makeup_water',
thermo=water_thermo,
price=price['Makeup water'])
def test_stream():
import thermosteam as tmo
tmo.settings.set_thermo(['Water'], cache=True)
stream = tmo.Stream(None, Water=1, T=300)
assert [stream.chemicals.Water] == stream.available_chemicals
assert_allclose(stream.epsilon, 77.70030000000003)
assert_allclose(stream.alpha * 1e6, 0.14330776454124503)
assert_allclose(stream.nu, 8.799123532986536e-07)
assert_allclose(stream.Pr, 6.14001869413997)
assert_allclose(stream.Cn, 75.29555729396768)
assert_allclose(stream.C, 75.29555729396768)
assert_allclose(stream.Cp, 4.179538552493643)
assert_allclose(stream.P_vapor, 3533.918074415897)
assert_allclose(stream.mu, 0.0008766363688287887)
assert_allclose(stream.kappa, 0.5967303492959747)
assert_allclose(stream.rho, 996.2769195618362)
assert_allclose(stream.V, 1.80826029854462e-05)
assert_allclose(stream.H, 139.31398526921475)
assert_allclose(stream.S, 70.46581776376684)
assert_allclose(stream.sigma, 0.07176932405246211)
assert_allclose(stream.z_mol, [1.0])
assert_allclose(stream.z_mass, [1.0])
assert_allclose(stream.z_vol, [1.0])
assert not stream.source
assert not stream.sink
assert stream.main_chemical == 'Water'
assert not stream.isfeed()
assert not stream.isproduct()
assert stream.vapor_fraction == 0.
with pytest.raises(ValueError):
stream.get_property('isfeed', 'kg/hr')
with pytest.raises(ValueError):
stream.set_property('invalid property', 10, 'kg/hr')
with pytest.raises(ValueError):
tmo.Stream(None, Water=1, units='kg')
stream.mol = 0.
stream.mass = 0.
stream.vol = 0.
with pytest.raises(AttributeError):
stream.F_mol = 1.
with pytest.raises(AttributeError):
stream.F_mass = 1.
with pytest.raises(AttributeError):
stream.F_vol = 1.
# Make sure energy balance is working correctly with mix_from and vle
chemicals = tmo.Chemicals(['Water', 'Ethanol'])
thermo = tmo.Thermo(chemicals)
tmo.settings.set_thermo(thermo)
s3 = tmo.Stream('s3', T=300, P=1e5, Water=10, units='kg/hr')
s4 = tmo.Stream('s4', phase='g', T=400, P=1e5, Water=10, units='kg/hr')
s_eq = tmo.Stream('s34_mixture')
s_eq.mix_from([s3, s4])
s_eq.vle(H=s_eq.H, P=1e5)
H_sum = s3.H + s4.H
H_eq = s_eq.H
assert_allclose(H_eq, H_sum, rtol=1e-3)
s_eq.vle(H=s3.H + s4.H, P=1e5)
assert_allclose(s_eq.H, H_sum, rtol=1e-3)
def create_system(ID='wheatstraw_sys'):
System.maxiter = 400
System.converge_method = 'Aitken'
System.molar_tolerance = 0.01
### Streams ###
chemicals = bst.settings.get_chemicals()
non_soluble = [
'Xylan', 'Glucan', 'Arabinan', 'Lignin', 'Extract', 'Ash', 'Mannan',
'Galactan', 'Acetate'
]
# feed flow
drycomposition = chemicals.kwarray(
dict(Glucan=0.3342,
Xylan=0.2330,
Arabinan=0.0420,
Lignin=0.2260,
Extract=0.1330,
Ash=0.0180,
Acetate=0.0130))
TS = 0.95
moisture_content = chemicals.kwarray(dict(Water=1 - TS))
dryflow = 83333.0
netflow = dryflow / TS
feedflow = netflow * (drycomposition * TS + moisture_content)
process_water_over_dryflow = 19.96
sulfuric_acid_over_dryflow = 0.04
wheatstraw = Stream('wheatstraw',
feedflow,
units='kg/hr',
price=price['Feedstock'] * TS)
# %% Pretreatment system
process_water1 = Stream(
'process_water1',
T=25 + 273.15,
P=1 * 101325,
Water=process_water_over_dryflow * dryflow, #only an initialization
units='kg/hr')
sulfuric_acid = Stream('sulfuric_acid',
P=1 * 101325,
T=25 + 273.15,
Water=0.05 * sulfuric_acid_over_dryflow * dryflow,
SulfuricAcid=0.95 * sulfuric_acid_over_dryflow *
dryflow,
units='kg/hr',
price=price['Sulfuric acid'] * 0.95)
steam = Stream(
'steam',
phase='g',
T=212 + 273.15,
P=20 * 101325,
Water=dryflow * 0.5, #This is just a guess
units='kg/hr')
U101 = units.FeedStockHandling('U101', ins=wheatstraw)
U101.cost_items['System'].cost = 0
T201 = units.SulfuricAcidTank('T201', ins=sulfuric_acid)
M201 = bst.Mixer('M201', ins=(process_water1, T201 - 0, Stream()))
M202 = units.WashingTank('M202', ins=(M201 - 0, U101 - 0))
S200 = units.SieveFilter('S200',
ins=(M202 - 0),
outs=(Stream('feed_20TS'),
Stream('recycled_water1')),
moisture_content=1 - 0.20,
split=find_split_solids(M202 - 0, non_soluble))
S201 = units.PressureFilter('S201',
ins=(S200 - 0),
outs=(Stream('feed_50TS'),
Stream('recycled_water2')),
moisture_content=0.5,
split=find_split_solids(S200 - 0, non_soluble))
M200 = bst.Mixer('M200', ins=(S200 - 1, S201 - 1), outs='recycled_water')
M200 - 0 - 2 - M201
recycled_water = M200 - 0
def update_process_water1():
process_water1.imass[
'Water'] = process_water_over_dryflow * dryflow - recycled_water.imass[
'Water']
sulfuric_acid.imass[
'SulfuricAcid'] = 0.95 * sulfuric_acid_over_dryflow * dryflow - recycled_water.imass[
'SulfuricAcid']
sulfuric_acid.imass[
'Water'] = 0.05 / 0.95 * sulfuric_acid.imass['SulfuricAcid']
water_recycle_sys = System('water_recycle_sys',
path=(U101, T201, M201, M202, S200, S201, M200,
update_process_water1),
recycle=M201 - 0)
M205 = bst.Mixer('M205', ins=(S201 - 0, None))
M203 = units.SteamMixer('M203',
ins=(M205 - 0, steam),
P=steam.chemicals.Water.Psat(190.0 + 273.15))
R201 = units.PretreatmentReactorSystem(
'R201',
ins=M203 - 0,
outs=(Stream('pretreatment_steam'), Stream('pretreatment_effluent')))
P201 = units.BlowdownDischargePump('P201', ins=R201 - 1)
T202 = units.OligomerConversionTank('T202', ins=P201 - 0)
F201 = units.PretreatmentFlash('F201',
ins=T202 - 0,
outs=(Stream('flash_steam'),
Stream('flash_effluent')),
P=101325,
Q=0)
M204 = bst.Mixer('M204', ins=(R201 - 0, F201 - 0))
S202 = units.PressureFilter('S202',
ins=(F201 - 1),
outs=(Stream('pretreated_stream'),
Stream('pretreated_liquid')),
moisture_content=0.5,
split=find_split_solids(F201 - 1, non_soluble))
S203 = bst.Splitter('S203',
ins=M204 - 0,
outs=(Stream('steam_back'), Stream('residual_steam')),
split=0.25)
H201 = units.WasteVaporCondenser('H201',
ins=S203 - 1,
outs=Stream('condensed_steam'),
T=99 + 273.15,
V=0)
S203 - 0 - 1 - M205
steam_out1 = S203 - 1
steam_inS203 = 0 - S203
steam_out0 = S203 - 0
def update_split():
steam_out1.mol[:] = steam_inS203.mol[:] - steam_out0.mol[:]
pretreatment_sys = System(
'pretreatment_sys',
path=(
water_recycle_sys, M205, M203, R201, P201, T202, F201, M204, S202,
S203, update_split,
H201), # TODO: H201 moved to the end, no need to resimulate system
recycle=M204 - 0)
### TODO: There is a bug in original code; for now spec is constant
# S203.split[:] = 0.5
T90 = 90 + 273.15
def f_DSpret(split):
S203.split[:] = split
for i in range(3):
pretreatment_sys.simulate()
sobj = M205 - 0
return sobj.T - T90
pretreatment_sys.specification = BoundedNumericalSpecification(
f_DSpret, 0.10, 0.70)
### Fermentation system ###
cellulase_conc = 0.05
cellulase = Stream('cellulase', units='kg/hr', price=price['Enzyme'])
ammonia = Stream(
'ammonia',
Ammonia=1051 / 1000 * dryflow, #This is just a initialization
units='kg/hr',
phase='l',
price=price['Ammonia'])
process_water2 = Stream(
'process_water2',
T=10 + 273.15,
P=1 * 101325,
Water=1664.8 / 1000 * dryflow, #This is just a guess
units='kg/hr')
ammonia1 = Stream(
'ammonia1',
Ammonia=26 / 1000 * dryflow, #This is just a initialization
units='kg/hr',
price=price['Ammonia'])
ammonia2 = Stream(
'ammonia2',
Ammonia=116 / 1000 * dryflow, #This is just a initialization
units='kg/hr',
price=price['Ammonia'])
ammonia_fresh = Stream('ammonia_fresh',
units='kg/hr',
price=price['Ammonia'])
ammonia_storage = units.DAPTank('Ammonia_storage',
ins=ammonia_fresh,
outs='Ammonia_fermentation')
S301 = bst.ReversedSplitter('S301',
ins=ammonia_storage - 0,
outs=(ammonia, ammonia1, ammonia2))
air1 = Stream('air_lagoon1', O2=51061, N2=168162, phase='g', units='kg/hr')
air2 = Stream('air_lagoon2', O2=51061, N2=168162, phase='g', units='kg/hr')
J1 = bst.Junction('J1', upstream=S202 - 0, downstream=Stream())
sacch_split = 0.05 #This is just a initialization
ammonia_zmass = 0.0052
M301 = bst.Mixer('M301', ins=(ammonia, process_water2))
M302 = bst.Mixer('M302', ins=(J1 - 0, M301 - 0))
S303 = units.PressureFilter('S303',
ins=(M302 - 0),
outs=(Stream('cooled_hydrolysate'),
Stream('residual_water')),
moisture_content=0.4,
split=find_split_solids(M302 - 0, non_soluble))
WIS_prehyd = 0.20
cooled_hydrolyzate_pre = M302.outs[0]
S303_out0 = S303.outs[0]
S303_out1 = S303.outs[1]
def update_moisture_content():
F_non_sol_S303in = find_WIS(
cooled_hydrolyzate_pre,
non_soluble) * cooled_hydrolyzate_pre.F_mass
F_sol_S303in = cooled_hydrolyzate_pre.F_mass - F_non_sol_S303in
F_sol_S303out = F_non_sol_S303in / WIS_prehyd - cellulase.F_mass - F_non_sol_S303in
split_soluble = F_sol_S303out / F_sol_S303in
new_split = find_split_solids(cooled_hydrolyzate_pre, non_soluble)
new_split[new_split == 0] = split_soluble
S303_out0.mass[:] = cooled_hydrolyzate_pre.mass[:] * new_split
S303_out1.mass[:] = cooled_hydrolyzate_pre.mass[:] * (1 - new_split)
T203 = units.AmmoniaAdditionTank('T203', ins=S303 - 0)
M303 = units.EnzymeHydrolysateMixer('M303', ins=(T203 - 0, cellulase))
cellulase_over_WIS = 0.05 * cellulase_conc
water_over_WIS = 0.05 * (1 - cellulase_conc)
def update_cellulase_and_nutrient_loading():
WIS_premixer = cooled_hydrolyzate_pre.F_mass * find_WIS(
cooled_hydrolyzate_pre, non_soluble)
cellulase_mass = cellulase_over_WIS * WIS_premixer
water_mass = water_over_WIS * WIS_premixer
cellulase.imass['Cellulase'] = cellulase_mass * 1.1
cellulase.imass['Water'] = water_mass * 1.1
# Note: An additional 10% is produced for the media glucose/sophorose mixture
# Humbird (2011) p[g. 37
def update_ammonia_loading():
water_cooled_hydrolyzate = cooled_hydrolyzate_pre.imass['Water']
ammonia.F_mass = water_cooled_hydrolyzate * ammonia_zmass
M304 = bst.Mixer('M304', ins=(M303 - 0, None))
R301 = units.SaccharificationAndCoFermentation(
'R301',
ins=(M304 - 0, ammonia1, air1),
outs=(Stream('CO2_1'), Stream('fermentation_slurry'),
Stream('saccharified_to_seed')),
saccharified_slurry_split=sacch_split)
M305 = bst.Mixer('M305', ins=(R301 - 2, ammonia2, air2))
R302 = units.SeedTrain('R302',
ins=M305 - 0,
outs=(Stream('CO2_2'), Stream('effluent')))
T301 = units.SeedHoldTank('T301', ins=R302 - 1)
T301 - 0 - 1 - M304
air2_over_glucose = (R302.reactions.X[1] * 2.17 + R302.reactions.X[3] *
1.5 / 2 - R302.reactions.X[2]) * 1.1
ammonia2_over_glucose = R302.reactions.X[1] * 0.62 * 1.1
preseed = M305 - 0
def update_nutrient_loading2():
glucose_preseed = preseed.imol['Glucose']
air2.imol['O2'] = air2_over_glucose * glucose_preseed
air2.imol['N2'] = (air2_over_glucose * glucose_preseed) / 0.21 * 0.79
ammonia2_mol = ammonia2_over_glucose * glucose_preseed - preseed.imol[
'Ammonia']
if ammonia2_mol < 0:
ammonia2.imol['NH3'] = 0
else:
ammonia2.imol['NH3'] = ammonia2_mol
air1_over_glucose = (R301.cofermentation.X[1] * 2.17 +
R301.cofermentation.X[3] * 1.5 / 2 -
R301.cofermentation.X[2]) * 1.2
ammonia1_over_glucose = R301.cofermentation.X[1] * 0.62 * 1.1
preferm = M304 - 0
glucose_over_glucan = R301.saccharification.X[
0] + R301.saccharification.X[1] * 0.5 + R301.saccharification.X[2]
def update_nutrient_loading1():
glucose_preferm = preferm.imol['Glucan'] * glucose_over_glucan * (
1 - R301.saccharified_slurry_split)
air1.imol['O2'] = air1_over_glucose * glucose_preferm
air1.imol['N2'] = (air1_over_glucose * glucose_preferm) / 0.21 * 0.79
ammonia1_mol = ammonia1_over_glucose * glucose_preferm - preferm.imol[
'Ammonia'] * (1 - R301.saccharified_slurry_split)
if ammonia1_mol < 0:
ammonia1.imol['NH3'] = 0
else:
ammonia1.imol['NH3'] = ammonia1_mol
# TODO: Bug in update nutrient loading (not enough O2 to run R301 and R302 seed train)
# TODO: so just ignore negative flow in the meanwhile
# def ignore_negative_O2_flow():
# for i in (R301.outs + R302.outs): i.imol['O2'] = 0
seed_recycle_sys = System('seed_recycle_sys',
path=(M304, update_nutrient_loading1, R301, M305,
update_nutrient_loading2, R302, T301),
recycle=M304 - 0)
conc_yeast = 3.0
def f_DSferm1(x):
sacch_split = x
R301.saccharified_slurry_split = sacch_split
for i in range(3):
seed_recycle_sys.simulate()
s_obj2 = R301 - 1
light_ind = s_obj2.chemicals._light_indices
l = [a for a in s_obj2.vol[light_ind] if not a == 0]
v_0 = s_obj2.F_vol - sum(l)
conc_yeast_obtained = s_obj2.imass['S_cerevisiae'] / v_0
return ((conc_yeast_obtained - conc_yeast) / conc_yeast)
seed_recycle_sys.specification = BoundedNumericalSpecification(
f_DSferm1, 0.01, 0.35)
fermentation_sys = System(
'fermentation_sys',
path=(J1, M301, M302, S303, update_ammonia_loading, T203,
update_cellulase_and_nutrient_loading, update_moisture_content,
M303, seed_recycle_sys)) #update_moisture_content,
T_solid_cool = 50.0 + 273.15
def f_DSferm2(x):
mass_water = x
process_water2.F_mass = mass_water
for i in range(3):
fermentation_sys.simulate()
s_obj1 = M302 - 0
return ((s_obj1.T - T_solid_cool) / T_solid_cool)
fermentation_sys.specification = BoundedNumericalSpecification(
f_DSferm2, process_water2.F_mass / 2, process_water2.F_mass * 2)
### Ethanol purification ###
stripping_water = Stream(
'stripping_water',
Water=26836, #This is just a initialization
units='kg/hr')
M306 = bst.Mixer('M306', ins=(R302 - 0, R301 - 0))
T302 = units.BeerTank('T302', outs=Stream('cool_feed'))
# tmo.Stream.default_ID_number = 400
M401 = bst.Mixer('M401', ins=(R301 - 1, None))
M401 - 0 - T302
D401 = bst.VentScrubber('D401',
ins=(stripping_water, M306 - 0),
outs=(Stream('CO2_purified'),
Stream('bottom_liquid')),
gas=('CO2', 'NH3', 'O2', 'N2'))
D401 - 1 - 1 - M401
# Heat up before beer column
# Exchange heat with stillage
mid_eth_massfrac = 0.50
high_eth_massfrac = 0.915
bott_eth_massfrac = 0.00001
dist_high_pres = 2 * 101325
high_dist_stream = Stream('high_eth_stream',
Ethanol=high_eth_massfrac,
Water=1 - high_eth_massfrac,
units='kg/hr')
mid_dist_stream = Stream('mid_eth_stream',
Ethanol=mid_eth_massfrac,
Water=1 - mid_eth_massfrac,
units='kg/hr')
bottom_stream = Stream(
'bottom_stream',
Ethanol=
bott_eth_massfrac, #only an initialization. Later it gets updated with the real composition
Water=1 - bott_eth_massfrac,
units='kg/hr')
dist_high_dp = high_dist_stream.dew_point_at_P(dist_high_pres)
bott_mid_dp = bottom_stream.dew_point_at_T(dist_high_dp.T - 5)
dist_mid_dp = mid_dist_stream.dew_point_at_P(bott_mid_dp.P)
bott_low_dp = bottom_stream.dew_point_at_T(dist_mid_dp.T - 5)
dist_low_dp = mid_dist_stream.dew_point_at_P(bott_low_dp.P)
S401 = bst.Splitter('S401',
ins=(T302 - 0),
outs=(Stream('feed_low_pressure', P=bott_low_dp.P),
Stream('feed_mid_pressure', P=bott_mid_dp.P)),
split=0.5)
H402 = bst.HXprocess('H402',
ins=(S401 - 0, None),
outs=(Stream('warmed_feed_lp'),
Stream('cooled_bottom_water_lp')),
U=1.28)
H403 = bst.HXprocess('H403',
ins=(S401 - 1, None),
outs=(Stream('warmed_feed_mp'),
Stream('cooled_bottom_water_mp')),
U=1.28)
# Beer column
Ethanol_MW = chemicals.Ethanol.MW
Water_MW = chemicals.Water.MW
def Ethanol_molfrac(e):
"""Return ethanol mol fraction in a ethanol water mixture"""
return e / Ethanol_MW / (e / Ethanol_MW + (1 - e) / Water_MW)
xbot = Ethanol_molfrac(bott_eth_massfrac)
ytop = Ethanol_molfrac(mid_eth_massfrac)
D402 = units.DistillationColumn('D402',
ins=H402 - 0,
P=bott_low_dp.P,
y_top=ytop,
x_bot=xbot,
k=1.5,
LHK=('Ethanol', 'Water'),
energy_integration=True)
D402.tray_material = 'Stainless steel 304'
D402.vessel_material = 'Stainless steel 304'
D402.BM = 2.4
D402.boiler.U = 1.85
# Condense distillate
H402_dist = bst.HXutility('H402_dist',
ins=D402 - 0,
V=0,
T=dist_low_dp.T - 1)
P402_2 = bst.Pump('P402_2', ins=H402_dist - 0, P=bott_mid_dp.P)
P402_2.BM = 3.1
D402 - 1 - 1 - H402
LP_dist_sys = System('LP_dist_sys',
path=(H402, D402, H402_dist),
recycle=H402 - 0)
D403 = units.DistillationColumn('D403',
ins=H403 - 0,
P=bott_mid_dp.P,
y_top=ytop,
x_bot=xbot,
k=1.5,
LHK=('Ethanol', 'Water'),
energy_integration=True)
D403.tray_material = 'Stainless steel 304'
D403.vessel_material = 'Stainless steel 304'
D403.BM = 2.4
D403.boiler.U = 1.85
# Condense distillate
H403_dist = bst.HXutility('H403_dist',
ins=D403 - 0,
V=0,
T=dist_mid_dp.T - 1)
D403 - 1 - 1 - H403
MP_dist_sys = System('MP_dist_sys',
path=(H403, D403, H403_dist),
recycle=H403 - 0)
M402 = bst.Mixer('M402',
ins=(P402_2 - 0, H403_dist - 0),
outs=Stream(P=bott_mid_dp.P))
P404 = bst.Pump('P404', ins=M402 - 0, P=dist_high_pres)
M403 = bst.Mixer('M403',
ins=(H402 - 1, H403 - 1),
outs=Stream('bottom_water'))
S402 = units.PressureFilter('S402',
ins=(M403 - 0),
outs=(Stream('Lignin'),
Stream('Thin_spillage')),
flux=1220.6 * 0.8,
moisture_content=0.35,
split=find_split_solids(M403 - 0, non_soluble))
# Mix ethanol Recycle (Set-up)
M404 = bst.Mixer('M404',
ins=(P404 - 0, None),
outs=Stream(P=dist_high_pres))
ytop = Ethanol_molfrac(high_eth_massfrac)
D404 = units.DistillationColumn('D404',
ins=M404 - 0,
P=dist_high_pres,
y_top=ytop,
x_bot=xbot,
k=1.5,
LHK=('Ethanol', 'Water'),
energy_integration=True)
D404.tray_material = 'Stainless steel 304'
D404.vessel_material = 'Stainless steel 304'
D404.BM = 2.4
D404.boiler.U = 1.85
P405 = bst.Pump('P405', ins=D404 - 1, outs=Stream('bottom_water'))
# Superheat vapor for mol sieve
H404 = bst.HXutility('H404', ins=D404 - 0, T=dist_high_dp.T + 37.0, V=1)
# Molecular sieve
U401 = bst.MolecularSieve('U401',
ins=H404 - 0,
split=(2165.14 / 13356.04, 1280.06 / 1383.85),
order=('Ethanol', 'Water'))
U401 - 0 - 1 - M404
ethanol_recycle_sys = System('ethanol_recycle_sys',
path=(M404, D404, H404, U401),
recycle=M404 - 0)
# Condense ethanol product
H405 = bst.HXutility('H405', ins=U401 - 1, V=0, T=dist_high_dp.T - 1)
T701 = bst.StorageTank('T701',
ins=H405 - 0,
tau=7 * 24,
vessel_type='Floating roof',
vessel_material='Carbon steel')
ethanol = Stream('ethanol', price=price['Ethanol'])
P701 = bst.Pump('P701', ins=T701 - 0, outs=ethanol)
P701.BM = 3.1
T701.BM = 1.7
vent_stream = M306 - 0
stripping_water_over_vent = stripping_water.mol / 21202.490455845436
def update_stripping_water():
stripping_water.mol[:] = stripping_water_over_vent * vent_stream.F_mass
purification_sys = System(
'purification_sys',
path=(M306, update_stripping_water, D401, M401, T302, S401,
MP_dist_sys, LP_dist_sys, P402_2, M402, P404, M403, S402,
ethanol_recycle_sys, P405, H405, T701, P701))
def f_DSpur(split):
S401.split[:] = split
for i in range(3):
purification_sys.simulate()
heat_cond = D403.condenser.Q + H403_dist.Q
heat_boil = D402.boiler.Q
return heat_boil + heat_cond #heat_boil and heat_cond have different signs
purification_sys.specification = BoundedNumericalSpecification(
f_DSpur, 0.10, 0.70)
### Biogas production
organic_groups = [
'OtherSugars', 'SugarOligomers', 'OrganicSolubleSolids', 'Furfurals',
'OtherOrganics', 'Protein', 'CellMass'
]
organics = list(
sum([chemical_groups[i] for i in organic_groups],
('Ethanol', 'AceticAcid', 'Xylose', 'Glucose', 'ExtractVol',
'ExtractNonVol')))
organics.remove('WWTsludge')
P_sludge = 0.05 / 0.91 / chemicals.WWTsludge.MW
MW = np.array([chemicals.CH4.MW, chemicals.CO2.MW])
CH4_molcomp = 0.60
mass = np.array([CH4_molcomp, 1 - CH4_molcomp]) * MW
mass /= mass.sum()
mass *= 0.381 / (0.91)
P_ch4, P_co2 = mass / MW
def anaerobic_rxn(reactant):
MW = getattr(chemicals, reactant).MW
return rxn.Reaction(
f"{1/MW}{reactant} -> {P_ch4}CH4 + {P_co2}CO2 + {P_sludge}WWTsludge",
reactant, 0.91)
anaerobic_digestion = rxn.ParallelReaction(
[anaerobic_rxn(i) for i in organics] +
[rxn.Reaction(f"H2SO4 -> H2S + 2O2", 'H2SO4', 1.)])
well_water1 = Stream('well_water1', Water=1, T=15 + 273.15)
J5_1 = bst.Junction('J5_1', upstream=S303 - 1, downstream=Stream())
J5_2 = bst.Junction('J5_2', upstream=S402 - 1, downstream=Stream())
J5_3 = bst.Junction('J5_3', upstream=S202 - 1, downstream=Stream())
J5_4 = bst.Junction('J5_4', upstream=H201 - 0, downstream=Stream())
J5_5 = bst.Junction('J5_5', upstream=P405 - 0, downstream=Stream())
M501 = bst.Mixer('M501',
ins=(J5_1 - 0, J5_2 - 0, J5_3 - 0, J5_4 - 0, J5_5 - 0))
splits = [('Ethanol', 1, 15), ('Water', 27158, 356069), ('Glucose', 3, 42),
('Xylose', 7, 85), ('OtherSugars', 13, 175),
('SugarOligomers', 10, 130), ('OrganicSolubleSolids', 182, 2387),
('InorganicSolubleSolids', 8, 110), ('Ammonia', 48, 633),
('AceticAcid', 0, 5), ('Furfurals', 5, 70),
('OtherOrganics', 9, 113), ('Cellulose', 19, 6), ('Xylan', 6, 2),
('OtherStructuralCarbohydrates', 1, 0), ('Lignin', 186, 64),
('Protein', 51, 18), ('CellMass', 813, 280),
('OtherInsolubleSolids', 68, 23)]
raw_biogas = Stream('raw_biogas', price=price['Pure biogas'] * 0.33)
Tin_digestor = 37 + 273.15
R501 = units.AnaerobicDigestion('R501',
ins=(M501 - 0, well_water1),
outs=(raw_biogas, 'waste_effluent',
'sludge_effluent', ''),
reactions=anaerobic_digestion,
sludge_split=find_split(*zip(*splits)),
T=Tin_digestor)
digestor_sys = System('digestor_sys',
path=(J5_1, J5_2, J5_3, J5_4, J5_5, M501, R501))
### Waste water treatment
combustion = chemicals.get_combustion_reactions()
def growth(reactant):
f = chemicals.WWTsludge.MW / getattr(chemicals, reactant).MW
return rxn.Reaction(f"{f}{reactant} -> WWTsludge", reactant, 1.)
# Note, nitrogenous species included here, but most of it removed in R601 digester
aerobic_digestion = rxn.ParallelReaction([
i * 0.74 + 0.22 * growth(i.reactant) for i in combustion
if (i.reactant in organics)
])
aerobic_digestion.X[:] = 0.96
# tmo.Stream.default_ID_number = 600
well_water = Stream('well_water', Water=1, T=15 + 273.15)
raw_biogas2 = Stream('raw_biogas2', price=price['Pure biogas'] * 0.33)
WWTC = units.WasteWaterSystemCost('WWTC', ins=R501 - 1)
R601 = units.AnaerobicDigestionWWT('R601',
ins=(WWTC - 0, well_water),
outs=(raw_biogas2, '', '', ''),
reactions=anaerobic_digestion,
sludge_split=find_split(*zip(*splits)),
T=Tin_digestor - 2)
air = Stream('air_lagoon', O2=51061, N2=168162, phase='g', units='kg/hr')
caustic = Stream('WWT_caustic',
Water=2252,
NaOH=2252,
units='kg/hr',
price=price['Caustic'] * 0.5)
# polymer = Stream('WWT polymer') # Empty in humbird report :-/
M602 = bst.Mixer('M602', ins=(R601 - 1, None))
caustic_over_waste = caustic.mol / 2544300.6261793654
air_over_waste = air.mol / 2544300.6261793654
waste = M602 - 0
def update_aerobic_input_streams():
F_mass_waste = waste.F_mass
caustic.mol[:] = F_mass_waste * caustic_over_waste
air.mol[:] = F_mass_waste * air_over_waste
R602 = units.AerobicDigestionWWT('R602',
ins=(waste, air, caustic),
outs=('evaporated_water', ''),
reactions=aerobic_digestion)
splits = [('Ethanol', 0, 1), ('Water', 381300, 2241169), ('Glucose', 0, 2),
('Xylose', 1, 3), ('OtherSugars', 1, 7),
('SugarOligomers', 1, 6), ('OrganicSolubleSolids', 79, 466),
('InorganicSolubleSolids', 4828, 28378), ('Ammonia', 3, 16),
('Furfurals', 0, 3), ('OtherOrganics', 1, 7),
('CarbonDioxide', 6, 38), ('O2', 3, 17), ('N2', 5, 32),
('Cellulose', 0, 194), ('Xylan', 0, 65),
('OtherStructuralCarbohydrates', 0, 15), ('Lignin', 0, 1925),
('Protein', 0, 90), ('CellMass', 0, 19778),
('OtherInsolubleSolids', 0, 707)]
S601 = bst.Splitter('S601', ins=R602 - 1, split=find_split(*zip(*splits)))
S602 = bst.Splitter('S602', ins=S601 - 1, split=0.96)
M603 = bst.Mixer('M603', ins=(S602 - 0, None))
M603 - 0 - 1 - M602
M604 = bst.Mixer('M604', ins=(R601 - 2, S602 - 1))
centrifuge_species = ('Water', 'Glucose', 'Xylose', 'OtherSugars',
'SugarOligomers', 'OrganicSolubleSolids',
'InorganicSolubleSolids', 'Ammonia', 'Furfurals',
'OtherOrganics', 'CO2', 'COxSOxNOxH2S', 'Cellulose',
'Xylan', 'OtherStructuralCarbohydrates', 'Lignin',
'Protein', 'CellMass', 'OtherInsolubleSolids')
S623_flow = np.array(
[7708, 0, 0, 1, 1, 13, 75, 3, 0, 1, 1, 2, 25, 8, 2, 250, 52, 1523, 92])
S616_flow = np.array([
109098, 3, 6, 13, 9, 187, 1068, 46, 5, 8, 14, 31, 1, 0, 0, 13, 3, 80, 5
])
S603 = bst.Splitter('S603',
ins=M604 - 0,
outs=('', 'sludge'),
split=find_split(centrifuge_species, S616_flow,
S623_flow))
S603 - 0 - 1 - M603
S604 = bst.Splitter('S604',
ins=S601 - 0,
outs=('treated_water', 'waste_brine'),
split={'Water': 0.987})
aerobic_recycle_sys = System('aerobic_recycle_sys',
path=(M602, update_aerobic_input_streams,
R602, S601, S602, M604, S603, M603),
recycle=M602 - 0)
WWT_sys = System('WWT_sys', path=(WWTC, R601, aerobic_recycle_sys, S604))
### Facilities
# %% Facilities
# TODO: Double check that I did is right.
# TODO: The BoilerTurbogenerator burns both biogas and lignin
# Note that lime and boilerchems cost is taking into account in the
# unit operation now
# M605 = bst.Mixer('M605', ins=(R501-0, R601-0))
BT = bst.facilities.BoilerTurbogenerator(
'BT',
ins=(S402 - 0, '', 'boiler_makeup_water', 'natural_gas', 'lime',
'boilerchems'),
turbogenerator_efficiency=0.85)
# tmo.Stream.default_ID_number = 700
CWP = bst.facilities.ChilledWaterPackage('CWP')
CT = bst.facilities.CoolingTower('CT')
CT.outs[1].T = 273.15 + 28
water_thermo = tmo.Thermo(tmo.Chemicals(['Water']))
process_water = tmo.Stream(ID='process_water', thermo=water_thermo)
process_water_streams = (caustic, stripping_water, process_water1,
process_water2, steam, BT - 1, CT - 1)
def update_water_loss():
process_water.imol['Water'] = sum(
[i.imol['Water'] for i in process_water_streams])
makeup_water = Stream('makeup_water',
thermo=water_thermo,
price=price['Makeup water'])
PWC = bst.facilities.ProcessWaterCenter(
'PWC',
ins=(S604 - 0, makeup_water),
outs=(process_water, ''),
makeup_water_streams=(makeup_water, ),
process_water_streams=process_water_streams)
Substance = tmo.Chemical.blank('Substance')
Substance.at_state(phase='l')
Substance.default()
substance_thermo = tmo.Thermo(tmo.Chemicals([Substance]))
CIP = Stream('CIP',
thermo=substance_thermo,
flow=(126 / 83333 * dryflow, ))
CIP_package = units.CIPpackage('CIP_package',
ins=CIP,
thermo=substance_thermo)
plant_air = Stream('plant_air',
flow=(83333 / 83333 * dryflow, ),
thermo=substance_thermo)
ADP = bst.facilities.AirDistributionPackage('ADP',
ins=plant_air,
thermo=substance_thermo)
FT = units.FireWaterTank('FT',
ins=Stream('fire_water',
flow=(8343 / 83333 * dryflow, ),
thermo=substance_thermo),
thermo=substance_thermo)
### Complete system
wheatstraw_sys = System('wheatstraw_sys',
path=(pretreatment_sys, fermentation_sys,
ammonia_storage, S301, purification_sys,
digestor_sys, WWT_sys),
facilities=(CWP, BT, CT, update_water_loss, PWC,
ADP, CIP_package, S301,
ammonia_storage, FT))
return wheatstraw_sys
def set_thermo(self, thermo):
"""Set the default Thermo object. If `thermo` is not a Thermo object,
an attempt is made to convert it to one."""
if not isinstance(thermo, tmo.Thermo):
thermo = tmo.Thermo(thermo)
self._thermo = thermo