def create_stream(self, ID):
"""
Create stream from data.
Parameters
----------
ID=None : str
ID of stream to create.
"""
data = self.stream_data[ID]
return tmo.Stream(ID, **data) if data else tmo.Stream(ID)
def __init__(self, ID='', ins=None, outs=(), saccharified_slurry_split = 0.1, P=101325):
Unit.__init__(self, ID, ins, outs)
self.P = P
# Split to outs[2]
self.saccharified_slurry_split = saccharified_slurry_split
#: [ParallelReaction] Enzymatic hydrolysis reactions including from downstream batch tank in co-fermentation.
self.saccharification = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucan -> GlucoseOligomer', 'Glucan', 0.0400),
Rxn('Glucan + 0.5 H2O -> 0.5 Cellobiose', 'Glucan', 0.0120),
Rxn('Glucan + H2O -> Glucose', 'Glucan', 0.8000),#changed
Rxn('GlucoseOligomer + H2O -> Glucose', 'GlucoseOligomer', 1.0000),
Rxn('Cellobiose + H2O -> Glucose', 'Cellobiose', 1.0000),
Rxn('Xylan -> XyloseOligomer', 'Xylan', 0.0400),
Rxn('Xylan + H2O -> Xylose', 'Xylan', 0.9000)
])
self.loss = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucose -> 2 LacticAcid', 'Glucose', 0.0300),
Rxn('3 Xylose -> 5 LacticAcid', 'Xylose', 0.0300),
Rxn('3 Arabinose -> 5 LacticAcid', 'Arabinose', 0.0300),
Rxn('Galactose -> 2 LacticAcid', 'Galactose', 0.0300),
Rxn('Mannose -> 2 LacticAcid', 'Mannose', 0.0300),])
self.cofermentation = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucose -> 2 Ethanol + 2 CO2', 'Glucose', 0.8300),#changed
Rxn('Glucose + 0.62 NH3 + 2.17 O2 -> 3.65 S_cerevisiae + 3.71 H2O + 2.34 CO2', 'Glucose', 0.0130),
Rxn('Glucose + 2 H2O -> 2 Glycerol + O2', 'Glucose', 0.0040),
Rxn('2 Glucose + 1.5 O2 -> 3 SuccinicAcid + 3 H2O', 'Glucose', 0.0060),
])
self.saccharified_stream = tmo.Stream(None)
def get_grouped_chemicals(stream, units='kmol/hr'):
new_stream = tmo.Stream(stream.thermo)
new_stream.set_flow(stream.mol, units, stream.chemicals.IDs)
data = {
group: new_stream.get_flow(units, IDs).sum()
for group, IDs in chemical_groups.items()
}
return pd.Series(data)
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, 77.72395675564552)
assert_allclose(stream.alpha * 1e6, 0.1462889847474686)
assert_allclose(stream.nu, 8.596760626756933e-07)
assert_allclose(stream.Pr, 5.876560454361681)
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, 0.0008564676992124578)
assert_allclose(stream.kappa, 0.609138593165859)
assert_allclose(stream.rho, 996.2679390499142)
assert_allclose(stream.V, 1.808276598480142e-05)
assert_allclose(stream.H, 139.3139852692184)
assert_allclose(stream.S, 0.4658177637668395)
assert_allclose(stream.sigma, 0.07168596252716256)
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.
def create_streams(self, IDs=None):
"""
Create streams from data.
Parameters
----------
IDs=None : Iterable[str], optional
IDs of streams to create. Defaults to all streams.
"""
data = self.stream_data
if IDs: data = {i:data[i] for i in as_IDs(IDs)}
return [tmo.Stream(i, **(j or {})) for i, j in data.items()]
def test_reaction_enthalpy_balance():
# Combustion; ensure heat of gas phase reaction without sensible heats is
# the lower heating value
chemicals = H2O, Methane, CO2, O2, H2 = tmo.Chemicals(['H2O', 'Methane', 'CO2', 'O2', 'H2'])
H2O.H.g.Hvap_Tb = 44011.496 # Depending on the model, this value may be different.
tmo.settings.set_thermo(chemicals)
combustion = tmo.Reaction('Methane + O2 -> H2O + CO2',
reactant='Methane', X=1,
correct_atomic_balance=True)
Tref = 298.15
Tb = H2O.Tb
feed = tmo.Stream(Methane=1, O2=2, T=Tb, phase='g')
H0 = feed.Hnet - Methane.Cn.g.T_dependent_property_integral(Tref, Tb) - 2 * O2.Cn.g.T_dependent_property_integral(Tref, Tb)
combustion(feed)
Hf = feed.Hnet - 2 * H2O.Cn.l.T_dependent_property_integral(Tref, Tb) - CO2.Cn.g.T_dependent_property_integral(Tref, Tb)
assert_allclose(Hf - H0, -Methane.LHV)
# Electrolysis of water; ensure heat of reaction without sensible
# heats is the higher heating value of hydrogen (with opposite sign)
tmo.settings.set_thermo(chemicals)
reaction = tmo.Reaction('2H2O,l -> 2H2,g + O2,g', reactant='H2O', X=1)
feed = tmo.Stream(None, H2O=1)
H0 = feed.Hnet
feed.phases = ('g', 'l') # Gas and liquid phases must be available
reaction(feed) # Call to run reaction on molar flow
Hf = feed.Hnet
assert_allclose(Hf - H0, H2.HHV)
# Electrolysis of water; ensure gas phase heat of reaction without sensible
# heats is the lower heating value of hydrogen (with opposite sign)
reaction = tmo.Reaction('2H2O -> 2H2 + O2', reactant='H2O', X=1)
feed = tmo.Stream(None, H2O=1, T=Tref, phase='g')
H0 = feed.Hnet - H2O.Cn.l.T_dependent_property_integral(Tref, H2O.Tb) - H2O.Cn.g.T_dependent_property_integral(H2O.Tb, Tref)
reaction(feed) # Call to run reaction on molar flow
Hf = feed.Hnet
assert_allclose(Hf - H0, H2.LHV)
def __init__(self, ID='', ins=None, outs=(), P=101325):
Unit.__init__(self, ID, ins, outs)
self.P = P
#: [ParallelReaction] Enzymatic hydrolysis reactions including from downstream batch tank in co-fermentation.
self.saccharification = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucan -> GlucoseOligomer', 'Glucan', 0.0400),
Rxn('Glucan + 0.5 H2O -> 0.5 Cellobiose', 'Glucan', 0.0120),
Rxn('Glucan + H2O -> Glucose', 'Glucan', 0.9000),
Rxn('Cellobiose + H2O -> Glucose', 'Cellobiose', 1.0000)])
self.loss = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucose -> 2 LacticAcid', 'Glucose', 0.0300),
Rxn('3 Xylose -> 5 LacticAcid', 'Xylose', 0.0300),
Rxn('3 Arabinose -> 5 LacticAcid', 'Arabinose', 0.0300),
Rxn('Galactose -> 2 LacticAcid', 'Galactose', 0.0300),
Rxn('Mannose -> 2 LacticAcid', 'Mannose', 0.0300),])
self.cofermentation = ParallelRxn([
# Reaction definition Reactant Conversion
Rxn('Glucose -> 2 Ethanol + 2 CO2', 'Glucose', 0.9500),
Rxn('Glucose + 0.047 CSL + 0.018 DAP -> 6 Z_mobilis + 2.4 H2O', 'Glucose', 0.0200),
Rxn('Glucose + 2 H2O -> 2 Glycerol + O2', 'Glucose', 0.0040),
Rxn('Glucose + 2 CO2 -> 2 SuccinicAcid + O2', 'Glucose', 0.0060),
Rxn('3 Xylose -> 5 Ethanol + 5 CO2', 'Xylose', 0.8500),
Rxn('Xylose + 0.039 CSL + 0.015 DAP -> 5 Z_mobilis + 2 H2O',
'Xylose', 0.0190),
Rxn('3 Xylose + 5 H2O -> 5 Glycerol + 2.5 O2', 'Xylose', 0.0030),
Rxn('Xylose + H2O -> Xylitol + 0.5 O2', 'Xylose', 0.0460),
Rxn('3 Xylose + 5 CO2 -> 5 SuccinicAcid + 2.5 O2', 'Xylose', 0.0090),
])
self.CSL2constituents = Rxn(
'CSL -> 0.5 H2O + 0.25 LacticAcid + 0.25 Protein', 'CSL', 1.0000)
self.saccharified_stream = tmo.Stream(None)
# %% 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'])
PWC = bst.facilities.ProcessWaterCenter('PWC',
def create_system(ID='cornstover_sys'):
System.maxiter = 400
System.converge_method = 'Aitken'
System.molar_tolerance = 0.01
### Streams ###
chemicals = bst.settings.get_chemicals()
# feed flow
dry_composition = chemicals.kwarray(
dict(Glucan=0.3505,
Xylan=0.1953,
Lignin=0.1576,
Ash=0.0493,
Acetate=0.0181,
Protein=0.0310,
Extract=0.1465,
Arabinan=0.0238,
Galactan=0.0143,
Mannan=0.0060,
Sucrose=0.0077))
moisture_content = chemicals.kwarray(dict(Water=0.20))
netflow = 104167.0
feedflow = netflow * (dry_composition * 0.8 + moisture_content)
cornstover = Stream('cornstover',
feedflow,
units='kg/hr',
price=price['Feedstock'])
warm_process_water = Stream('warm_process_water',
T=368.15,
P=4.7 * 101325,
Water=140000,
units='kg/hr')
ammonia_process_water = Stream('ammonia_process_water',
T=368.15,
P=4.7 * 101325,
Water=150310,
units='kg/hr')
rectifier_bottoms_product = Stream('',
T=100 + 273.15,
P=101325,
Ethanol=18,
Water=36629,
Furfural=72,
HMF=100,
units='kg/hr')
sulfuric_acid = Stream('sulfuric_acid',
P=5.4 * 101325,
T=294.15,
Water=139,
SulfuricAcid=1842,
units='kg/hr',
price=price['Sulfuric acid'])
steam = Stream('steam',
phase='g',
T=268 + 273.15,
P=13 * 101325,
Water=24534 + 3490,
units='kg/hr')
ammonia = Stream('ammonia',
Ammonia=1051,
units='kg/hr',
phase='l',
price=price['Ammonia'])
cellulase = Stream('cellulase', units='kg/hr', price=price['Enzyme'])
### Pretreatment system
U101 = units.FeedStockHandling('U101', cornstover)
U101.cost_items['System'].cost = 0
T201 = units.SulfuricAcidTank('T201', sulfuric_acid)
M201 = units.SulfuricAcidMixer('M201',
(rectifier_bottoms_product, T201 - 0))
M202 = bst.Mixer('M202', (M201 - 0, warm_process_water, U101 - 0))
M203 = units.SteamMixer('M203', (M202 - 0, steam), P=5.5 * 101325)
R201 = units.PretreatmentReactorSystem('R201', M203 - 0)
P201 = units.BlowdownDischargePump('P201', R201 - 1)
T202 = units.OligomerConversionTank('T202', P201 - 0)
F201 = units.PretreatmentFlash('F201', T202 - 0, P=101325, Q=0)
M204 = bst.Mixer('M204', (R201 - 0, F201 - 0))
H201 = units.WasteVaporCondenser('H201', M204 - 0, T=99 + 273.15, V=0)
M210 = units.AmmoniaMixer('M210', (ammonia, ammonia_process_water))
M205 = bst.Mixer('M205', (F201 - 1, M210 - 0))
T203 = units.AmmoniaAdditionTank('T203', M205 - 0)
P209 = units.HydrolyzatePump('P209', T203 - 0)
H301 = units.HydrolysateCooler('H301', P209 - 0, T=48 + 273.15)
M301 = units.EnzymeHydrolysateMixer('M301', (H301 - 0, cellulase))
def update_pretreatment_process_water():
warm_process_water.imass[
'Water'] = 140000.0 * M202.ins[2].F_mass / 104175.33336
sulfuric_acid_over_feed = sulfuric_acid.mol / cornstover.F_mass
def update_sulfuric_acid_loading():
# Also plant air
F_mass_feed = cornstover.F_mass
plant_air.mol[0] = 0.8 * F_mass_feed
sulfuric_acid.mol[:] = sulfuric_acid_over_feed * F_mass_feed
hydrolyzate = F201.outs[1]
ammonia_over_hydrolyzate = ammonia.mol / 310026.22446428984
def update_ammonia_loading():
ammonia.mol[:] = ammonia_over_hydrolyzate * hydrolyzate.F_mass
ammonia_process_water.imass[
'Water'] = ammonia.imass['Ammonia'] * 150310 / 1051
cooled_hydrolyzate = H301.outs[0]
enzyme_over_cellulose = 20 / 1000 * 20 # (20 g enzyme / cellulose) / (50 g cellulase / 1 L enzyme)
water_cellulase_mass = cellulase.imass['Water', 'Cellulase']
water_cellulase_to_cellulase = np.array([0.95, 0.05])
def update_cellulase_and_nutrient_loading():
F_mass_cooled_hydrolyzate = cooled_hydrolyzate.F_mass
cellulose = cornstover.imass['Glucan']
# Note: An additional 10% is produced for the media glucose/sophorose mixture
# Humbird (2011) pg. 37
water_cellulase_mass[:] = (enzyme_over_cellulose *
water_cellulase_to_cellulase * cellulose *
1.1)
DAP1.mol[:] = DAP1_over_hydrolyzate * F_mass_cooled_hydrolyzate
DAP2.mol[:] = DAP2_over_hydrolyzate * F_mass_cooled_hydrolyzate
CSL1.mol[:] = CSL1_over_hydrolyzate * F_mass_cooled_hydrolyzate
CSL2.mol[:] = CSL2_over_hydrolyzate * F_mass_cooled_hydrolyzate
pretreatment_sys = System('pretreatment_sys',
path=(U101, T201, M201,
update_pretreatment_process_water, M202,
M203, R201, P201, T202, F201, M204, H201,
M210, M205, T203, P209, T203, H301, M301))
### Fermentation system ###
DAP1 = Stream('DAP1', DAP=26, units='kg/hr', price=price['DAP'])
DAP2 = Stream('DAP2', DAP=116, units='kg/hr', price=price['DAP'])
DAP_storage = units.DAPTank('DAP_storage', Stream('DAP_fresh'), outs='DAP')
S301 = bst.ReversedSplitter('S301', DAP_storage - 0, outs=(DAP1, DAP2))
CSL1 = Stream('CSL1', CSL=211, units='kg/hr', price=price['CSL'])
CSL2 = Stream('CSL2', CSL=948, units='kg/hr', price=price['CSL'])
CSL_storage = units.CSLTank('CSL_storage', Stream('CSL_fresh'), outs='CSL')
S302 = bst.ReversedSplitter('S302', CSL_storage - 0, outs=(CSL1, CSL2))
denaturant = Stream('denaturant',
Octane=230.69,
units='kg/hr',
price=price['Denaturant'])
stripping_water = Stream('stripping_water', Water=26836, units='kg/hr')
DAP1_over_hydrolyzate = DAP1.mol / 451077.22446428984
DAP2_over_hydrolyzate = DAP2.mol / 451077.22446428984
CSL1_over_hydrolyzate = CSL1.mol / 451077.22446428984
CSL2_over_hydrolyzate = CSL2.mol / 451077.22446428984
M302 = bst.Mixer('M302', (M301 - 0, None))
R301 = units.SaccharificationAndCoFermentation('R301',
(M302 - 0, CSL2, DAP2))
M303 = bst.Mixer('M303', (R301 - 2, CSL1, DAP1))
R302 = units.SeedTrain('R302', M303 - 0)
T301 = units.SeedHoldTank('T301', R302 - 1)
T301 - 0 - 1 - M302
fermentation_sys = System('fermentation_sys',
path=(update_cellulase_and_nutrient_loading,
M302, R301, M303, R302, T301),
recycle=M302 - 0)
### Ethanol purification ###
M304 = bst.Mixer('M304', (R302 - 0, R301 - 0))
T302 = units.BeerTank('T302')
M401 = bst.Mixer('M401', (R301 - 1, None))
M401 - 0 - T302
D401 = bst.VentScrubber('D401', (stripping_water, M304 - 0),
gas=('CO2', 'NH3', 'O2'))
D401 - 1 - 1 - M401
# Heat up before beer column
# Exchange heat with stillage
H401 = bst.HXprocess('H401', (T302 - 0, None),
phase0='l',
phase1='l',
U=1.28)
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)
# Beer column
xbot = Ethanol_molfrac(0.00001)
ytop = Ethanol_molfrac(0.50)
D402 = bst.BinaryDistillation('D402',
H401 - 0,
k=1.25,
Rmin=0.3,
P=101325,
y_top=ytop,
x_bot=xbot,
LHK=('Ethanol', 'Water'))
D402.tray_material = 'Stainless steel 304'
D402.vessel_material = 'Stainless steel 304'
D402.boiler.U = 1.85
P401 = bst.Pump('P401', D402 - 1)
P401 - 0 - 1 - H401
# Mix ethanol Recycle (Set-up)
M402 = bst.Mixer('M402', (D402 - 0, None))
ytop = Ethanol_molfrac(0.915)
D403 = bst.BinaryDistillation('D403',
M402 - 0,
Rmin=0.3,
P=101325,
y_top=ytop,
x_bot=xbot,
k=1.25,
LHK=('Ethanol', 'Water'))
D403.tray_material = 'Stainless steel 304'
D403.vessel_material = 'Stainless steel 304'
D403.is_divided = True
D403.boiler.U = 1.85
P402 = bst.Pump('P402', D403 - 1)
P402 - 0 - 0 - M201
# Superheat vapor for mol sieve
H402 = bst.HXutility('H402', D403 - 0, T=115 + 273.15, V=1)
# Molecular sieve
U401 = bst.MolecularSieve('U401',
H402 - 0,
split=(2165.14 / 13356.04, 1280.06 / 1383.85),
order=('Ethanol', 'Water'))
U401 - 0 - 1 - M402
ethanol_recycle_sys = System('ethanol_recycle_sys',
path=(M402, D403, H402, U401),
recycle=M402 - 0)
# Condense ethanol product
H403 = bst.HXutility('H403', U401 - 1, V=0, T=350.)
T701 = bst.StorageTank('T701',
H403 - 0,
tau=7 * 24,
vessel_type='Floating roof',
vessel_material='Carbon steel')
P701 = bst.Pump('P701', T701 - 0)
# Storage for gasoline
T702 = bst.StorageTank('T702',
denaturant,
tau=7 * 24,
vessel_type='Floating roof',
vessel_material='Carbon steel')
P702 = bst.Pump('P702', T702 - 0)
# Mix in denaturant
ethanol = Stream('ethanol', price=price['Ethanol'])
M701 = bst.MixTank('M701', (P702 - 0, P701 - 0), outs=ethanol)
M701.line = 'Mixer'
M701.tau = 0.05
def adjust_denaturant():
denaturant.imol['Octane'] = 0.022 * P701.outs[0].F_mass / 114.232
P401.BM = P402.BM = P701.BM = P702.BM = 3.1
T701.BM = T702.BM = 1.7
vent_stream = M304 - 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
puresys = System('purification',
path=(M304, update_stripping_water, D401, M401, T302,
H401, D402, H401, P401, H401, ethanol_recycle_sys,
P402, H403, T701, P701, adjust_denaturant, T702,
P702, M701))
### Lignin Separation
recycled_water = tmo.Stream(Water=1,
T=47 + 273.15,
P=3.9 * 101325,
units='kg/hr')
splits = [('Glucose', 19, 502), ('Xylose', 40, 1022),
('OtherSugars', 81, 2175), ('SugarOligomers', 60, 1552),
('OrganicSolubleSolids', 612, 15808),
('InorganicSolubleSolids', 97, 2513), ('Furfurals', 19, 513),
('OtherOrganics', 52, 1348), ('Glucan', 1230, 25),
('Xylan', 415, 8), ('OtherStructuralCarbohydrates', 94, 2),
('Lignin', 12226, 250), ('Protein', 3376, 69),
('CellMass', 925, 19), ('OtherInsolubleSolids', 4489, 92)]
S401 = units.PressureFilter('S401', ('', recycled_water),
moisture_content=0.35,
split=find_split(*zip(*splits)))
H401 - 1 - 0 - S401
### 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.)
organic_groups = [
'OtherSugars', 'SugarOligomers', 'OrganicSolubleSolids', 'Furfurals',
'OtherOrganics', 'Protein', 'CellMass'
]
organics = list(
sum([chemical_groups[i] for i in organic_groups],
('Ethanol', 'AceticAcid', 'Xylose', 'Glucose')))
organics.remove('WWTsludge')
P_sludge = 0.05 / 0.91 / chemicals.WWTsludge.MW
MW = np.array([chemicals.CH4.MW, chemicals.CO2.MW])
mass = np.array([0.51, 0.49]) * MW
mass /= mass.sum()
mass *= 0.86 / (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)
# TODO: Revise this with Jeremy
anaerobic_digestion = rxn.ParallelReaction(
[anaerobic_rxn(i) for i in organics] +
[rxn.Reaction("H2SO4 -> H2S + 2O2", 'H2SO4', 1.)])
# Note, nitogenous species included here, but most of it removed in R601 digester
# TODO: Add ammonium to reaction, make sure it can be a liquid, possibly add Henry's constant
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
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)]
well_water = Stream('well_water', Water=1, T=15 + 273.15)
M601 = bst.Mixer('M601', (S401 - 1, '', ''))
H201 - 0 - 1 - M601
WWTC = units.WasteWaterSystemCost('WWTC', M601 - 0)
R601 = units.AnaerobicDigestion('R601', (WWTC - 0, well_water),
reactions=anaerobic_digestion,
sludge_split=find_split(*zip(*splits)))
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', (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.AerobicDigestion('R602', (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', R602 - 1, split=find_split(*zip(*splits)))
S602 = bst.Splitter('S602', S601 - 1, split=0.96)
M603 = bst.Mixer('M603', (S602 - 0, None))
M603 - 0 - 1 - M602
M604 = bst.Mixer('M604', (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',
M604 - 0,
outs=('', 'sludge'),
split=find_split(centrifuge_species, S616_flow,
S623_flow))
S603 - 0 - 1 - M603
S604 = bst.Splitter('S604',
S601 - 0,
outs=('treated_water', 'waste_brine'),
split={'Water': 0.987})
aerobic_digestion_sys = System('aerobic_digestion_sys',
path=(M602, update_aerobic_input_streams,
R602, S601, S602, M604, S603, M603),
recycle=M602 - 0)
### Facilities
M501 = bst.Mixer('M501', (S603 - 1, S401 - 0))
BT = bst.facilities.BoilerTurbogenerator(
'BT',
ins=(M501 - 0, R601 - 0, 'boiler_makeup_water', 'natural_gas', 'lime',
'boilerchems'),
turbogenerator_efficiency=0.85)
CWP = bst.facilities.ChilledWaterPackage('CWP')
CT = bst.facilities.CoolingTower('CT')
CT.outs[1].T = 273.15 + 28
process_water_streams = (caustic, stripping_water, warm_process_water,
steam, BT - 1, CT - 1)
makeup_water = Stream('makeup_water', price=price['Makeup water'])
PWC = bst.facilities.ProcessWaterCenter('PWC', (S604 - 0, makeup_water),
(), None, (BT - 1, CT - 1),
process_water_streams)
blowdown_mixer = bst.BlowdownMixer('blowdown_mixer', (BT - 1, CT - 1),
2**M601)
CIP = Stream('CIP', Water=126, units='kg/hr')
CIP_package = units.CIPpackage('CIP_package', CIP)
plant_air = Stream('plant_air', N2=83333, units='kg/hr')
ADP = bst.facilities.AirDistributionPackage('ADP', plant_air)
fire_water = Stream('fire_water', Water=8343, units='kg/hr')
FT = units.FireWaterTank('FT', fire_water)
### Complete system
cornstover_sys = System(ID,
path=(pretreatment_sys, fermentation_sys, puresys,
S401, M601, WWTC, R601,
aerobic_digestion_sys, S604),
facilities=(M501, CWP, BT, CT, PWC, ADP,
CIP_package, S301, S302, DAP_storage,
CSL_storage, FT, blowdown_mixer),
facility_recycle=blowdown_mixer - 0)
return cornstover_sys
def __init__(self,
ID='',
ins=None,
outs=(),
thermo=None,
P=101325,
*,
LHK,
k,
Rmin=0.3,
Lr=None,
Hr=None,
y_top=None,
x_bot=None,
product_specification_format=None,
vessel_material='Carbon steel',
tray_material='Carbon steel',
tray_type='Sieve',
tray_spacing=450,
stage_efficiency=None,
velocity_fraction=0.8,
foaming_factor=1.0,
open_tray_area_fraction=0.1,
downcomer_area_fraction=None,
is_divided=False):
Unit.__init__(self, ID, ins, outs, thermo)
# Operation specifications
self.k = k
self.P = P
self.Rmin = Rmin
self.LHK = LHK
self._set_distillation_product_specifications(
product_specification_format, x_bot, y_top, Lr, Hr)
# Construction specifications
self.vessel_material = vessel_material
self.tray_type = tray_type
self.tray_material = tray_material
self.tray_spacing = tray_spacing
self.stage_efficiency = stage_efficiency
self.velocity_fraction = velocity_fraction
self.foaming_factor = foaming_factor
self.open_tray_area_fraction = open_tray_area_fraction
self.downcomer_area_fraction = downcomer_area_fraction
self.is_divided = is_divided
# Setup components
thermo = self.thermo
#: [MultiStream] Overall feed to the distillation column
self.feed = tmo.MultiStream(None, thermo=thermo)
#: [HXutility] Condenser.
self.condenser = HXutility(None,
ins=tmo.Stream(None,
phase='g',
thermo=thermo),
outs=tmo.MultiStream(None, thermo=thermo),
thermo=thermo)
#: [HXutility] Boiler.
self.boiler = HXutility(None,
ins=tmo.Stream(None, thermo=thermo),
outs=tmo.MultiStream(None, thermo=thermo),
thermo=thermo)
self.heat_utilities = self.condenser.heat_utilities + self.boiler.heat_utilities
self.reset_cache()
def update_stripping_water():
stripping_water.mol[:] = stripping_water_over_vent * vent_stream.F_mass
puresys = System('purification',
path=(M304, update_stripping_water, D401, M401, T302, H401,
D402, H401, P401, H401, ethanol_recycle_sys, P402, H403,
T701, P701, adjust_denaturant, T702, P702, M701, JX))
# %% Lignin Separation
tmo.settings.set_thermo(cornstover_chemicals)
recycled_water = tmo.Stream(Water=1,
T=47 + 273.15,
P=3.9 * 101325,
units='kg/hr')
splits = [('Glucose', 19, 502), ('Xylose', 40, 1022),
('OtherSugars', 81, 2175), ('SugarOligomers', 60, 1552),
('OrganicSolubleSolids', 612, 15808),
('InorganicSolubleSolids', 97, 2513), ('Furfurals', 19, 513),
('OtherOrganics', 52, 1348), ('Glucan', 1230, 25), ('Xylan', 415, 8),
('OtherStructuralCarbohydrates', 94, 2), ('Lignin', 12226, 250),
('Protein', 3376, 69), ('CellMass', 925, 19),
('OtherInsolubleSolids', 4489, 92)]
# tmo.Stream.default_ID_number = IDnum_400
S401 = units.PressureFilter('S401',
ins=('', recycled_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
