def test_kolmogorov_smirnov_d(model):
# Test made by Yalin.
import numpy as np
import biosteam as bst
from chaospy import distributions as shape
bst.settings.set_thermo(['H2O', 'Ethanol'], cache=True)
s1 = bst.Stream('s1', H2O=100)
M1 = bst.MixTank(ins=s1)
M2 = bst.MixTank(ins=M1 - 0)
sys = bst.System('sys', path=(M1, M2))
model = bst.Model(sys)
baseline = 1
distribution = shape.Uniform(lower=0.5, upper=1.5)
@model.parameter(name='M1 tau',
element=M1,
kind='coupled',
distribution=distribution,
units='hr',
baseline=baseline)
def set_M1_tau(i):
M1.tau = i
baseline = 1.75
distribution = shape.Uniform(lower=1, upper=2)
@model.parameter(name='M2 tau',
element=M2,
kind='coupled',
distribution=distribution,
units='hr',
baseline=baseline)
def set_M2_tau(i):
M2.tau = i
model.metrics = [
bst.Metric(name='tau1', getter=lambda: M1.tau, units='hr', element=M1),
bst.Metric(name='tau2', getter=lambda: M2.tau, units='hr', element=M2),
]
np.random.seed(3221)
samples = model.sample(100, rule='L')
model.load_samples(samples)
model.evaluate()
D, p = model.kolmogorov_smirnov_d(
thresholds=[1, 1.5]) # Just make sure it works for now
def system():
bst.main_flowsheet.clear()
MockChemical = bst.Chemical('MockChemical', phase='l', search_db=False, default=True)
bst.settings.set_thermo([MockChemical])
with bst.System('MockSystem') as system:
feed = bst.Stream('feed', MockChemical=1e6, units='kg/hr', price=0.150)
product = bst.Stream('product', price=0.151)
M1 = bst.MixTank('M1', feed, 's1')
H1 = bst.HXutility('H1', M1-0, product, T=325, V=0.)
system.simulate()
return system
# IDnum_400 = bst.Stream.default_ID_number
# bst.Stream.default_ID_number = 700
T701 = bst.StorageTank('T701', ins=H403 - 0)
T701.line = 'Ethanol storage'
T701.tau = 7 * 24
P701 = bst.Pump('P701', ins=T701 - 0)
# Storage for gasoline
T702 = bst.StorageTank('T702', ins=denaturant)
T702.tau = 7 * 24
P702 = bst.Pump('P702', ins=T702 - 0)
# Mix in denaturant
ethanol = Stream('ethanol', price=price['Ethanol'])
M701 = bst.MixTank('M701', ins=(P702 - 0, P701 - 0), outs=ethanol)
M701.line = 'Mixer'
M701.tau = 0.05
gas_index = denaturant.index('Octane')
def adjust_denaturant():
denaturant.mol[gas_index] = 0.022 * P701.outs[0].massnet / 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 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