def diagram(self, radius=0, upstream=True, downstream=True,
file=None, format='png', **graph_attrs):
"""
Display a `Graphviz <https://pypi.org/project/graphviz/>`__ diagram
of the unit and all neighboring units within given radius.
Parameters
----------
radius : int
Maxium number streams between neighbors.
downstream=True : bool, optional
Whether to show downstream operations
upstream=True : bool, optional
Whether to show upstream operations
file : Must be one of the following:
* [str] File name to save diagram.
* [None] Display diagram in console.
format : str
Format of file.
"""
if radius > 0:
neighborhood = self._neighborhood(radius, upstream, downstream)
neighborhood.add(self)
sys = bst.System('', neighborhood)
return sys.diagram('thorough', file, format, **graph_attrs)
f = self.get_digraph(format, **graph_attrs)
finalize_digraph(f, file, format)
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
def build_network(self):
units = self.path + [self.sink]
network = []
for segment in units:
if isinstance(segment, list):
source = segment[0]
for recycle in segment[-1].outs:
if recycle.sink is source: break
system = bst.System(segment, recycle=recycle)
network.append(system)
else:
network.append(segment)
return network
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 test_parameter_hook():
import biosteam as bst
from chaospy.distributions import Uniform
sys = bst.System(None, ())
model = bst.Model(sys)
@model.parameter(distribution=Uniform(0., 1.), hook=round)
def set_param(x):
pass
np.random.seed(0)
samples = model.sample(10, 'L')
model.load_samples(samples)
actual_values = [[1.], [0.], [0.], [0.], [0.], [0.], [1.], [1.], [1.],
[1.]]
assert_allclose(model.table.values, actual_values)
def create_tea(sys, OSBL_units, ignored_units=()):
BT = tmo.utils.get_instance(OSBL_units,
bst.facilities.BoilerTurbogenerator)
OSBL_units = list(OSBL_units)
OSBL_units.remove(BT)
ethanol_tea = CellulosicEthanolTEA(
system=sys,
IRR=0.10,
duration=(2007, 2037),
depreciation='MACRS7',
income_tax=0.35,
operating_days=350.4,
lang_factor=None,
construction_schedule=(0.08, 0.60, 0.32),
startup_months=3,
startup_FOCfrac=1,
startup_salesfrac=0.5,
startup_VOCfrac=0.75,
WC_over_FCI=0.05,
finance_interest=0.08,
finance_years=10,
finance_fraction=0.4,
OSBL_units=OSBL_units, # BT not included
warehouse=0.04,
site_development=0.09,
additional_piping=0.045,
proratable_costs=0.10,
field_expenses=0.10,
construction=0.20,
contingency=0.10,
other_indirect_costs=0.10,
labor_cost=2.5e6,
labor_burden=0.90,
property_insurance=0.007,
maintenance=0.03)
for i in ignored_units:
ethanol_tea.units.remove(i)
ethanol_tea.units.remove(BT)
Area700 = bst.TEA.like(bst.System('Area700', (BT, )), ethanol_tea)
Area700.labor_cost = 0
Area700.depreciation = 'MACRS20'
Area700.OSBL_units = (BT, )
tea = bst.CombinedTEA([ethanol_tea, Area700], IRR=0.10)
sys._TEA = tea
return tea
def test_sanunit():
import biosteam as bst
from qsdsan import Components, WasteStream, sanunits
components = Components.load_default()
bst.settings.set_thermo(components)
ws1 = WasteStream(S_Ac=5, H2O=1000, units='kg/hr')
ws2 = WasteStream(X_NOO=10, H2O=1000, units='kg/hr')
M1 = sanunits.Mixer('M1', ins=(ws1, ws2, ''), outs='mixture')
M1.show()
assert type(M1.ins[0]).__name__ == 'WasteStream'
S1 = sanunits.Splitter('S1', ins=M1-0, outs=('', ''), split=0.2)
ins3 = WasteStream(S_CH3OH=7, H2O=1000, units='kg/hr')
P1 = sanunits.Pump('P1', ins=ins3)
M2 = sanunits.MixTank('M2', ins=(S1-0, P1-0), tau=2)
M2-0-2-M1
System = bst.System('System', path=(M1, S1, P1, M2), recycle=M2-0)
System.simulate()
assert_allclose(M2.installed_cost, 65519.00446342958, rtol=1e-3)
def create_evaluation_model():
import biosteam as bst
from chaospy.distributions import Uniform
sys = bst.System(None, ())
model = bst.Model(sys)
parameter_box = [100.]
@model.parameter(bounds=[90, 110],
distribution=Uniform(90, 110),
units='kg/hr')
def set_parameter(parameter_1):
parameter_box[0] = parameter_1
@model.parameter(bounds=[0., 1.], distribution=Uniform(0., 1.))
def set_parameter(parameter_2):
...
@model.metric
def good_metric():
p = parameter_box[0]
return 2. * p * p / (p + 100.)
switch_box = [False]
@model.metric
def bad_metric():
give_nan = switch_box[0]
switch_box[0] = not give_nan
p = parameter_box[0]
return float('Nan') if give_nan else 2. * p * p / (p + 100.)
@model.metric
def non_correlated_metric():
return float(switch_box[0])
sample = model.sample(1000, 'L')
model.load_samples(sample)
model.evaluate()
return model
def __call__(self, ID=None, ins=None, outs=None, mockup=False, area=None, udct=None,
operating_hours=None, **kwargs):
ins = create_streams(self.ins, ins, 'inlets', self.fixed_ins_size)
outs = create_streams(self.outs, outs, 'outlets', self.fixed_outs_size)
rename = area is not None
with (bst.MockSystem() if mockup else bst.System(ID or self.ID, operating_hours=operating_hours)) as system:
if rename:
unit_registry = system.flowsheet.unit
irrelevant_units = system._irrelevant_units
unit_registry.untrack(irrelevant_units)
self.f(ins, outs, **kwargs)
system.load_inlet_ports(ins, optional=[ins[i] for i in self.optional_ins_index])
system.load_outlet_ports(outs, optional=[outs[i] for i in self.optional_outs_index])
if rename:
units = system.units
if udct: unit_dct = {i.ID: i for i in units}
unit_registry.track(irrelevant_units)
utils.rename_units(units, area)
if udct: return system, unit_dct
elif udct:
unit_dct = {i.ID: i for i in system.units}
return system, unit_dct
return system
def create_fattyalcohol_production_sys(
ID='fattyalcohol_production_sys',
fa_stoichiometry='Glucose -> 1.5 Hexanol + 1.5 Octanol + 4.5 Decanol + H2O + CO2',
yg_stoichiometry='Glucose -> 3.72 Cells + 2 CO2'):
chemicals = tmo.settings.get_chemicals()
### Reactions ###
fatty_alcohol_production = Rxn(fa_stoichiometry,
'Glucose',
0.5,
basis='wt')
fatty_alcohol_production.basis = 'mol'
fatty_alcohol_production.correct_atomic_balance(constants=[
'Hexanol', 'Octanol', 'Decanol', 'Dodecanol', 'Tetradecanol'
])
yeast_growth = Rxn(yg_stoichiometry,
'Glucose',
.999,
correct_mass_balance=True)
### Streams ###
filepath = os.path.dirname(__file__)
stream_data_path = os.path.join(filepath, 'streams.yaml')
stream_data = tmo.ThermoData.from_yaml(stream_data_path)
glucose, process_water, tridecane, CSL, DAP, salt, \
cell_recycle, mixed_bioreactor_feed = stream_data.create_streams(
['glucose', 'process_water', 'tridecane', 'CSL', 'DAP',
'salt', 'cell_recycle', 'mixed_bioreactor_feed']
)
process_water.T = 310.15 # Assume heat integration so that this stream comes in heated
### Unit operations ###
M101 = units.Mixer('M101', ins=(tridecane, 'solvent_recycle'))
M101.ins[
1].T = 310.15 # Assume heat integration so that this stream comes in heated
one_week = 7 * 24
T101 = units.StorageTank('T101', glucose, tau=one_week)
T102 = units.StorageTank('T102', M101 - 0, tau=0.25)
P102 = units.Pump('P102', T102 - 0)
T103 = fa_units.CSLTank('T103', CSL)
T104 = units.StorageTank('T104', salt, tau=one_week)
T106 = fa_units.DAPTank('T106', DAP)
def balance_feeds_to_bioreactor():
feed_imol = mixed_bioreactor_feed.imol
glucose.imol['Glucose'] = feed_imol['Glucose']
process_water.imol[
'Water'] = feed_imol['Water'] - M101.ins[1].imol['Water']
tridecane.imol['Tridecane'] = feed_imol['Tridecane'] - M101.ins[
1].imol['Tridecane']
salt.imol['NaCl'] = feed_imol['NaCl']
cell_recycle.imol['Cells'] = feed_imol['Cells']
CSL.imol['CSL'] = feed_imol['CSL']
DAP.imol['DAP'] = feed_imol['DAP']
M101._run()
M101.specification = balance_feeds_to_bioreactor
M102 = units.Mixer('M102',
ins=(T101 - 0, P102 - 0, T103 - 0, T104 - 0, T106 - 0,
process_water, cell_recycle))
H101 = units.HXutility('H101',
ins=M102 - 0,
outs=mixed_bioreactor_feed,
material='Stainless steel/stainless steel',
T=310.15,
V=0)
def make_sure_enough_CSL_and_DAP_are_fed():
# tmo.reaction.CHECK_FEASIBILITY = False
feed = R101.ins[0]
CSL.imass['CSL'] = feed.imass['CSL'] = 0.0025 * feed.F_mass
DAP.imass['DAP'] = feed.imass['DAP'] = 0.33 * feed.F_vol
R101._run()
# effluent = R101.outs[1]
# if effluent.imol['CSL'] < 0. or effluent.imol['DAP'] < 0.:
# CSL.imol['CSL'] = feed.imol['CSL'] = CSL_flow - effluent.imol['CSL']
# DAP.imol['DAP'] = feed.imol['DAP'] = DAP_flow - effluent.imol['DAP']
# effluent.imol['CSL'] = effluent.imol['DAP'] = 0.
# tmo.reaction.CHECK_FEASIBILITY = True
R101 = fa_units.FattyAlcoholBioreactor(
'R101',
outs=('CO2', ''),
ins=H101 - 0,
fermentation_reaction=fatty_alcohol_production,
postfermentation_reaction=yeast_growth,
T=310.15,
tau=32,
V=3785,
Nmin=2,
Nmax=32)
R101.specification = make_sure_enough_CSL_and_DAP_are_fed
T105 = units.StorageTank('T105', ins=R101 - 1, tau=2)
solids_split = chemicals.kwarray({'Cells': 0.999})
solids_split[solids_split == 0] = 0.001
solids_split[chemicals.index('Water')] = 0
P104 = units.Pump('P104', ins=T105 - 0)
C101 = fa_units.SolidLiquidsSplitCentrifuge(
'C101',
ins=P104 - 0,
outs=('', 'aqueous_fraction', 'cell_mass'),
solids_split=solids_split,
liquids_split=dict(Water=0.0004,
Tridecane=0.9966,
Hexanol=0.6781,
Octanol=0.9608,
Decanol=0.9966,
Dodecanol=0.9999,
Tetradecanol=1.0),
moisture_content=0.45)
P107 = units.Pump('P107', C101 - 0, 'oil_fraction', P=5 * 101325)
### System ###
return bst.System(ID, (M101, T102, P102, T101, T104, T103, T106, M102,
H101, R101, T105, P104, C101, P107))
def diagram(self, radius=0, file=None, format='png'):
"""Display a `Graphviz <https://pypi.org/project/graphviz/>`__ diagram of the unit and all neighboring units within given radius.
**Parameters**
**radius:** [int] Maxium number streams between neighbors.
**file:** Must be one of the following:
* [str] File name to save diagram.
* [None] Display diagram in console.
**format:** Format of file.
"""
if radius > 0:
neighborhood = self._neighborhood(radius)
neighborhood.add(self)
sys = bst.System('', neighborhood)
return sys.diagram('thorough', file, format)
graphics = self._graphics
# Make a Digraph handle
f = Digraph(name='unit', filename='unit', format='svg')
f.attr('graph',
ratio='0.5',
splines='normal',
outputorder='edgesfirst',
nodesep='1.1',
ranksep='0.8',
maxiter='1000') # Specifications
f.attr(rankdir='LR') # Left to right
# If many streams, keep streams close
if (len(self.ins) >= 3) or (len(self.outs) >= 3):
f.attr('graph', nodesep='0.4')
# Initialize node arguments based on unit and make node
type_ = graphics.node_function(self) or self.line
name = self.ID + '\n' + type_
f.attr('node', **self._graphics.node)
f.node(name)
# Set stream node attributes
f.attr('node',
shape='rarrow',
fillcolor='#79dae8',
style='filled',
orientation='0',
width='0.6',
height='0.6',
color='black',
peripheries='1')
# Make nodes and edges for input streams
di = 0 # Destination position of stream
for stream in self.ins:
if not stream: continue
f.node(stream.ID)
edge_in = self._graphics.edge_in
if di >= len(edge_in): di = 0
f.attr('edge',
arrowtail='none',
arrowhead='none',
tailport='e',
**edge_in[di])
f.edge(stream.ID, name)
di += 1
# Make nodes and edges for output streams
oi = 0 # Origin position of stream
for stream in self.outs:
if not stream: continue
f.node(stream.ID)
edge_out = self._graphics.edge_out
if oi >= len(edge_out): oi = 0
f.attr('edge',
arrowtail='none',
arrowhead='none',
headport='w',
**edge_out[oi])
f.edge(name, stream.ID)
oi += 1
save_digraph(f, file, format)
def create_ethanol_production_system(ID='ethanol_production_sys',
sugar_solution=None):
### Streams ###
# Fresh water
stripping_water = bst.Stream('stripping_water', Water=5000, units='kg/hr')
# Gasoline
denaturant = bst.Stream('denaturant', Octane=230.69,
units='kg/hr', price=price['Gasoline'])
if not sugar_solution: # Feedstock
sugar_solution = bst.Stream('sugar_solution',
Glucose = 3802,
Sucrose = 4.309e+04,
Water = 2.59e+05,
H3PO4 = 83.33,
units = 'kg/hr',
T = 372,
)
# Yeast
yeast = bst.Stream('yeast', Water=24700, DryYeast=10300, units='kg/hr')
# Ethanol product
ethanol = bst.Stream('ethanol', price=price['Ethanol'])
### Units ###
# Split sugar solution
S301 = units.Splitter('S301',
split=0.265)
# Concentrate sugars
F301 = units.MultiEffectEvaporator('F301',
P=(101325, 73581, 50892, 32777),
V=0.95) # fraction evaporated
F301.components['condenser'].U = 1.85
# Note: value of steam ~ 6.86 for the following
# (101325, 73580.467, 50891.17, 32777.406, 19999.925, 11331.5),
# Mix sugar solutions
M301 = units.Mixer('M301')
# Cool for fermentation
H301 = units.HXutility('H301', T=295.15)
# Ethanol Production
R301 = units.Fermentation('R301', outs=('CO2', ''), tau=9, efficiency=0.90, N=4)
T301 = units.StorageTank('T301', tau=4, vessel_material='Carbon steel')
T301.line = 'Beer tank'
D301 = units.VentScrubber('D301', ins=(stripping_water, R301-0),
outs=('vent', ''),
gas=('CO2',))
# Separate 99% of yeast
C301 = units.SolidsCentrifuge('C301', outs=('', 'recycle_yeast'),
split=(1, 0.99999, 1, 0.96, 0.01),
order=('Ethanol', 'Glucose', 'H3PO4',
'Water', 'DryYeast'),
solids=('DryYeast',))
# Mix in Water
M302 = units.Mixer('M302')
P301 = units.Pump('P301')
# Heat up before beer column
# Exchange heat with stillage
H302 = units.HXprocess('H302', phase0='l', phase1='l', U=1.28)
# Beer column
xbot = mass2molar_ethanol_fraction(0.00001)
ytop = mass2molar_ethanol_fraction(0.574)
D302 = units.BinaryDistillation('D302', P=101325,
y_top=ytop, x_bot=xbot, k=1.25,
LHK=('Ethanol', 'Water'))
D302.tray_material = 'Stainless steel 304'
D302.vessel_material = 'Stainless steel 304'
D302.boiler.U = 1.85
P302 = units.Pump('P302')
# Mix ethanol Recycle (Set-up)
M303 = units.Mixer('M303')
ytop = mass2molar_ethanol_fraction(0.9061726)
D303 = units.BinaryDistillation('D303', P=101325,
y_top=ytop, x_bot=xbot, k=1.25,
LHK=('Ethanol', 'Water'),
tray_material='Stainless steel 304',
vessel_material='Stainless steel 304',
is_divided=True)
D303.boiler.U = 1.85
P303 = units.Pump('P303')
# Superheat vapor for mol sieve
H303 = units.HXutility('H303', T=115+273.15, V=1)
# Molecular sieve
U301 = units.MolecularSieve('U301',
split=(2165.14/13356.04, 1280.06/1383.85),
order=('Ethanol', 'Water'))
# Condense ethanol product
H304 = units.HXutility('H304', 'S149', V=0, T=340.)
T302 = units.StorageTank('T302', tau=7*24,
vessel_type='Floating roof',
vessel_material='Carbon steel')
P304 = units.Pump('P304')
# Storage for gasoline
T303 = units.StorageTank('T303', tau=7*24,
vessel_type='Floating roof',
vessel_material='Carbon steel')
P305 = units.Pump('P305')
# Denatured ethanol product
T304 = units.MixTank('T304', outs=ethanol)
T304.tau = 0.10
# Waste water
M305 = units.Mixer('M305', outs='wastewater')
# Yeast mixing
T305 = units.MixTank('T305')
T305.tau = 0.1
yeast-T305
# Multi-effect evaporator pumps
P306 = units.Pump('P306')
### Ethanol system set-up ###
sugar_solution-S301-1-F301-0-P306
(S301-0, P306-0)-M301-H301
(H301-0, yeast-T305-0)-R301-1-T301-0-C301
(C301-0, D301-1)-M302-P301
(P301-0, P302-0)-H302-0-D302-1-P302
(D302-0, U301-0)-M303-0-D303-0-H303-U301
D303-1-P303
def adjust_denaturant():
P304._run()
pure_ethanol = P304.outs[0]
denaturant.imol['Octane'] = 0.021*pure_ethanol.F_mass/114.232
P304.specification = adjust_denaturant
U301-1-H304-0-T302-0-P304
denaturant-T303-P305
(P305-0, P304-0)-T304
(P303-0, F301-1, H302-1)-M305
### System ###
return bst.System(ID,
[S301,
F301,
P306,
M301,
H301,
T305,
R301,
T301,
C301,
M302,
P301,
bst.System('beer_column_heat_integration',
[H302,
D302,
P302],
recycle=P302-0),
bst.System('ethanol_recycle_from_molecular_sieves',
[M303,
D303,
H303,
U301],
recycle=U301-0),
H304,
T302,
P304,
T303,
P305,
T304,
D301,
P303,
M305])
def create_system(ID='sugarcane_sys'):
### Streams ###
chemicals = bst.settings.get_chemicals()
z_mass_sugarcane = chemicals.kwarray(
dict(Glucose=0.0120811,
Lignin=0.0327653,
Solids=0.015,
Sucrose=0.136919,
Ash=0.006,
Cellulose=0.0611531,
Hemicellulose=0.036082,
Water=0.7))
sugarcane = bst.Stream('sugarcane',
flow=333334 * z_mass_sugarcane,
units='kg/hr',
price=price['Sugar cane'])
enzyme = bst.Stream('enzyme',
Cellulose=100,
Water=900,
units='kg/hr',
price=price['Protease'])
imbibition_water = bst.Stream('imbibition_water',
Water=87023.35,
units='kg/hr',
T=338.15)
H3PO4 = bst.Stream('H3PO4',
H3PO4=74.23,
Water=13.10,
units='kg/hr',
price=price['H3PO4']) # to T203
lime = bst.Stream('lime',
CaO=333.00,
Water=2200.00,
units='kg/hr',
price=price['Lime']) # to P5
polymer = bst.Stream('polymer',
Flocculant=0.83,
units='kg/hr',
price=price['Polymer']) # to T205
rvf_wash_water = bst.Stream('rvf_wash_water',
Water=16770,
units='kg/hr',
T=363.15) # to C202
### Unit operations ###
# Feed the shredder
U101 = units.ConveyingBelt('U101', ins=sugarcane)
# Separate metals
U102 = units.MagneticSeparator('U102', ins=U101 - 0)
# Shredded cane
U103 = units.Shredder('U103', ins=U102 - 0)
# Hydrolyze starch
T201 = units.EnzymeTreatment('T201', T=323.15) # T=50
# Finely crush lipid cane
U201 = units.CrushingMill('U201',
split=dict(Ash=0.92,
Cellulose=0.92,
Glucose=0.04,
Hemicellulose=0.92,
Lignin=0.92,
Sucrose=0.04,
Solids=1),
moisture_content=0.5)
# Convey out bagasse
U202 = units.ConveyingBelt('U202', ins=U201.outs[0], outs='Bagasse')
# Mix in water
M201 = units.Mixer('M201')
# crushing_mill_recycle_sys = bst.System('crushing_mill_recycle_sys',
# path=(U201, S201, M201),
# recycle=M201-0)
# Screen out fibers
S201 = units.VibratingScreen('S201',
split=dict(Ash=0.35,
Cellulose=0.35,
Glucose=0.88,
Hemicellulose=0.35,
Lignin=0.35,
Solids=0,
Sucrose=0.88,
Water=0.88))
# Store juice before treatment
T202 = units.StorageTank('T202', tau=4, vessel_material='Carbon steel')
# Heat up before adding acid
H201 = units.HXutility('H201', T=343.15)
# Mix in acid
T203 = units.MixTank('T203')
# Pump acid solution
P201 = units.Pump('P201')
# Mix lime solution
T204 = units.MixTank('T204', tau=0.10)
P202 = units.Pump('P202')
# Blend acid lipid solution with lime
T205 = units.MixTank('T205', tau=0.10)
# Mix recycle
M202 = units.Mixer('M202')
# Heat before adding flocculant
H202 = units.HXutility('H202', T=372.15)
# Mix in flocculant
T206 = units.MixTank('T206')
T206.tau = 0.10
# Separate residual solids
C201 = units.Clarifier('C201',
split=dict(Ash=0,
CaO=0,
Cellulose=0,
Flocculant=0.522,
Glucose=0.522,
Hemicellulose=0,
Lignin=0,
H3PO4=0.522,
Sucrose=0.522,
Water=0.522))
# Remove solids as filter cake
C202 = units.RVF('C202',
outs=('filter_cake', ''),
moisture_content=0.80,
split=dict(Ash=0.85,
CaO=0.85,
Cellulose=0.85,
Glucose=0.01,
Hemicellulose=0.85,
Lignin=0.85,
Sucrose=0.01))
P203 = units.Pump('P203')
# Screen out small fibers from sugar stream
S202 = units.VibratingScreen('S202',
outs=('', 'fiber_fines'),
split=dict(Ash=1.0,
CaO=1.0,
Cellulose=1.0,
Flocculant=0.0,
Glucose=0.998,
Hemicellulose=1.0,
Lignin=1.0,
H3PO4=1.0,
Sucrose=0.998,
Water=0.998))
S202.mesh_opening = 2
### Process specifications ###
# Specifications dependent on lipid cane flow rate
def correct_flows():
U103._run()
F_mass = sugarcane.F_mass
# correct enzyme, lime, phosphoric acid, and imbibition water
enzyme.imass['Cellulose',
'Water'] = 0.003 * F_mass * np.array([0.1, 0.9])
lime.imass['CaO', 'Water'] = 0.001 * F_mass * np.array([0.046, 0.954])
H3PO4.imass['H3PO4', 'Water'] = 0.00025 * F_mass
imbibition_water.imass['Water'] = 0.25 * F_mass
U103.specification = correct_flows
# Specifications within a system
def correct_wash_water():
P202._run()
solids = P202.outs[0].imol['Ash', 'CaO', 'Cellulose', 'Hemicellulose',
'Lignin'].sum()
rvf_wash_water.imol['Water'] = 0.0574 * solids
P202.specification = correct_wash_water
### System set-up ###
(U103 - 0, enzyme) - T201
(T201 - 0, M201 - 0) - U201 - 1 - S201 - 0 - T202
(S201 - 1, imbibition_water) - M201
T202 - 0 - H201
(H201 - 0, H3PO4) - T203 - P201
(P201 - 0, lime - T204 - 0) - T205 - P202
(P202 - 0, P203 - 0) - M202 - H202
(H202 - 0, polymer) - T206 - C201
(C201 - 1, rvf_wash_water) - C202 - 1 - P203
C201 - 0 - S202
### Ethanol section ###
ethanol_production_sys = create_ethanol_production_system(
sugar_solution=S202 - 0)
### Facilities ###
s = F.stream
BT = units.BoilerTurbogenerator(
'BT', (U202 - 0, '', 'boiler_makeup_water', 'natural_gas', '', ''),
boiler_efficiency=0.80,
turbogenerator_efficiency=0.85)
CT = units.CoolingTower('CT')
makeup_water_streams = (s.cooling_tower_makeup_water,
s.boiler_makeup_water)
process_water_streams = (s.imbibition_water, rvf_wash_water,
s.stripping_water, *makeup_water_streams)
makeup_water = bst.Stream('makeup_water', price=0.000254)
CWP = units.ChilledWaterPackage('CWP')
PWC = units.ProcessWaterCenter('PWC', (bst.Stream(), makeup_water), (),
None, makeup_water_streams,
process_water_streams)
### System ###
return bst.System(
ID,
[
U101, U102, U103, T201,
bst.System("juice_extraction_sys", [U201, S201, M201],
recycle=M201 - 0), T202, H201, T203, P201, T204, T205,
P202,
bst.System('juice_separation_sys',
[M202, H202, T206, C201, C202, P203],
recycle=P203 - 0), S202, ethanol_production_sys, U202
],
facilities=(CWP, BT, CT, PWC),
)
P306 = units.Pump('P306')
### Ethanol system set-up ###
sugar_solution - S301 - 1 - F301 - 0 - P306
(S301 - 0, P306 - 0) - M301 - H301
(H301 - 0, yeast - T305 - 0) - R301 - 1 - T301 - 0 - C301
(C301 - 0, D301 - 1) - M302 - P301
(P301 - 0, P302 - 0) - H302 - 0 - D302 - 1 - P302
EtOH_start_path = (S301, F301, P306, M301, H301, T305, R301, T301, C301, D301,
M302, P301, H302, D302, P302, H302)
(D302 - 0, U301 - 0) - M303 - 0 - D303 - 0 - H303 - U301
D303 - 1 - P303
ethanol_recycle_sys = bst.System('ethanol_recycle_sys',
path=(M303, D303, H303, U301),
recycle=M303 - 0)
pure_ethanol = P304.outs[0]
def adjust_denaturant():
denaturant.imol['Octane'] = 0.021 * pure_ethanol.F_mass / 114.232
PS4 = bst.ProcessSpecification('PS4', specification=adjust_denaturant)
U301 - 1 - H304 - 0 - T302 - 0 - P304 - 0 - PS4
denaturant - T303 - P305
(P305 - 0, PS4 - 0) - M304 - T304
(P303 - 0, F301 - 1) - M305
def test_equipment_lifetimes():
from biorefineries.sugarcane import create_tea
bst.settings.set_thermo(['Water'], cache=True)
class A(bst.Unit):
_BM = {
'Equipment A': 2,
'Equipment B': 3,
}
_equipment_lifetime = {
'Equipment A': 10,
'Equipment B': 5,
}
def _cost(self):
purchase_costs = self.purchase_costs
purchase_costs['Equipment A'] = 1e6
purchase_costs['Equipment B'] = 1e5
class B(bst.Unit):
_BM = {
'Equipment A': 2,
}
_equipment_lifetime = 15
def _cost(self):
self.purchase_costs['Equipment A'] = 1e6
class C(bst.Unit):
_BM = {
'Equipment A': 4,
}
def _cost(self):
self.purchase_costs['Equipment A'] = 1e6
@bst.decorators.cost('Flow rate', units='kmol/hr', S=1, BM=3,
cost=1e6, n=0.6, CE=bst.CE, lifetime=8)
class D(bst.Unit): pass
@bst.decorators.cost('Flow rate', units='kmol/hr', S=1, BM=4,
cost=1e6, n=0.6, CE=bst.CE, lifetime=20)
class E(bst.Unit): pass
D_feed = bst.Stream('D_feed', Water=1)
E_feed = D_feed.copy('E_feed')
units = [A(None, 'A_feed'), B(None, 'B_feed'), C(None, 'C_feed'), D(None, D_feed), E(None, E_feed)]
test_sys = bst.System('test_sys', units)
test_sys.simulate()
tea = create_tea(test_sys)
table = tea.get_cashflow_table()
C_FCI = table['Fixed capital investment [MM$]']
# Test with lang factor = 3 (default for sugarcane biorefinery)
cashflows_FCI = [6.12, 9.18, 0.0, 0.0, 0.0, 0.0, 0.0, 0.3, 0.0, 0.0, 3.0,
0.0, 3.3, 0.0, 0.0, 0.0, 0.0, 0.3, 0.0, 0.0, 0.0, 0.0]
assert_allclose(C_FCI, cashflows_FCI)
# Cashflows include maintainance and others, so all entries are not zero
cashflows = [-6120000.0, -9945000.0, -4321300.0, -4321300.0, -4321300.0,
-4321300.0, -4321300.0, -4621300.0, -4321300.0, -4321300.0,
-7321300.0, -4321300.0, -7621300.0, -4321300.0, -4321300.0,
-4321300.0, -4321300.0, -4621300.0, -4321300.0, -4321300.0,
-4321300.0, -3556300.0]
assert_allclose(tea.cashflow_array, cashflows)
# Test with bare module costs
tea.lang_factor = None
table = tea.get_cashflow_table()
C_FCI = table['Fixed capital investment [MM$]']
cashflows_FCI = [6.12, 9.18, 0.0, 0.0, 0.0, 0.0, 0.0, 0.3, 0.0, 0.0, 3.0,
0.0, 2.3, 0.0, 0.0, 0.0, 0.0, 0.3, 0.0, 0.0, 0.0, 0.0]
assert_allclose(C_FCI, cashflows_FCI)
cashflows = [-6120000.0, -9945000.0, -4321300.0, -4321300.0, -4321300.0,
-4321300.0, -4321300.0, -4621300.0, -4321300.0, -4321300.0,
-7321300.0, -4321300.0, -6621300.0, -4321300.0, -4321300.0,
-4321300.0, -4321300.0, -4621300.0, -4321300.0, -4321300.0,
-4321300.0, -3556300.0]
assert_allclose(tea.cashflow_array, cashflows)
def create_system(ID='LAOs_sys', stainless_steel=True):
checks = {'check_atomic_balance': True}
# LAOs production
LAOs_production = ParallelRxn([
Rxn('Hexanol -> Hexene + H2O', 'Hexanol', 1, **checks),
Rxn('Octanol -> Octene + H2O', 'Octanol', 1, **checks),
Rxn('Decanol -> Decene + H2O', 'Decanol', 1, **checks),
Rxn('Dodecanol -> Dodecene + H2O', 'Dodecanol', 1, **checks),
Rxn('Tetradecanol -> Tetradecene + H2O', 'Tetradecanol', 1, **checks),
Rxn('Hexadecanol -> Hexadecene + H2O', 'Hexadecanol', 1, **checks),
])
stream_data_path = os.path.join(os.path.dirname(__file__), 'streams.yaml')
stream_data = tmo.ThermoData.from_yaml(stream_data_path)
hexene, octene, decene = stream_data.create_streams(['hexene', 'octene', 'decene'])
fattyalcohol_production_sys = create_fattyalcohol_production_sys()
F.unit.C101.liquids_isplit['Hexene', 'Octene', 'Decene', 'Dodecene', 'Tetradecene'] = 1.0
H102 = units.HXprocess('H102', ins=F.unit.P107-0, dT=10, phase0='g', phase1='l')
M103 = units.Mixer('M103', ins=(H102-0, None))
H103 = units.HXutility('H103', ins=M103-0, V=1, T=623.15)
R102 = LAOs_units.AdiabaticFixedbedGasReactor('R102',
ins=H103-0,
WHSV=1.,
vessel_type='Vertical',
P=5 * 101325,
reaction=LAOs_production,
length_to_diameter=2,
catalyst_price=9.69,
catalyst_density=2650
)
R102-0-1-H102
R102.dehydration_reactor_mass_fraction = 0.10 # A proces specification
H105 = units.HXutility('H105', ins=H102-1, T=320)
T107 = LAOs_units.SurgeTank('T107', H105-0, ('recycle_nitrogen', 'LAOs_to_separations'),
tau=0.1)
P105 = units.Pump('P105', T107-1)
C102 = units.LiquidsSplitCentrifuge('C102', P105-0,
split=dict(Water=0.1,
Tridecane=1.0,
Hexene=1.0,
Octene=1.0,
Decene=1.0,
Dodecene=1.0,
Tetradecene=1.0))
P106 = units.Pump('P106', C102-0)
H104 = units.HXprocess('H104', ins=(P106-0, None), phase0='l', phase1='l')
# Lab mass fraction is 0.0242 g / g
# Baseline mass fraction is 0.1 g /g
def adjust_nitrogen_flow():
T107._run()
recycle_nitrogen = T107.outs[0]
feed = H102.outs[0]
F_mass = feed.F_mass
F_mass_alcohols = feed.imass[LAOs.fermentation_products].sum()
x_alcohol = R102.dehydration_reactor_mass_fraction
# Math to get amount of nitrogen flow:
# x_alcohol = F_mass_alcohols / (F_mass + F_mass_N2)
# F_mass_N2 * x_alcohol + x_alcohol * F_mass = F_mass_alcohols
# F_mass_N2 * x_alcohol = F_mass_alcohols - x_alcohol * F_mass
F_mass_N2 = F_mass_alcohols / x_alcohol - F_mass
if F_mass_N2 < 0: F_mass_N2 = 0
recycle_nitrogen.imass['Nitrogen'] = F_mass_N2
recycle_nitrogen.phase = 'g'
T107.specification = adjust_nitrogen_flow
T107 - 0 - 1 - M103
D101 = units.ShortcutColumn('D101', H104-0, LHK=('Decene', 'Tridecane'),
k=1.05, Lr=0.999, Hr=0.90, is_divided=True)
def distillate_recoveries_hook(IDs, recoveries):
light_keys = ('Water', 'Hexene', 'Octene')
index = [n for n, i in enumerate(IDs) if i in light_keys]
recoveries[index] = 1.0
D102 = units.ShortcutColumn('D102', D101-0, LHK=('Decene', 'Tridecane'),
k=1.05, y_top=0.98, x_bot=1e-9, is_divided=True)
D102._distillate_recoveries_hook = distillate_recoveries_hook
M105 = units.Mixer('M105', (D101-1, D102-1))
P108 = units.Pump('P108', M105-0)
P108-0-1-H104
settler_data = {'split': dict(Water=0.000227,
Tridecane=0.999999,
Hexanol=0.342,
Octanol=0.859,
Decanol=0.932,
Dodecanol=0.999,
Hexene=1.0,
Octene=1.0,
Decene=1.0,
Dodecene=1.0,
Tetradecene=1.0,
Tetradecanol=1.0)
}
M104 = units.MixerSettler('M104', (H104-1, F.unit.C101-1, C102-1, ''), ('', 'wastewater'),
settler_data=settler_data, model='split')
def adjust_price_per_organics():
M104._run()
wastewater = M104.outs[1]
wastewater.price = -0.33 * (1 - wastewater.imass['Water', 'NaCl'].sum() / wastewater.F_mass)
M104.specification = adjust_price_per_organics
M104.outs[1].price = -0.33 # USD / kg organics
P109 = units.Pump('P109', M104-0, 1**F.unit.M101)
H109 = units.HXutility('H109', D102-0, T=320, V=0)
C103 = units.LiquidsSplitCentrifuge('C103', H109-0, outs=('', 3**M104),
split=dict(Water=0.01,
Hexene=0.995,
Octene=0.999,
Decene=1.0,
Dodecene=1.0,
Tetradecene=1.0))
D103 = units.ShortcutColumn('D103', LHK=('Hexene', 'Octene'),
k=1.05, y_top=0.98, x_bot=1e-6)
H106 = units.HXutility('H106', D103-0, T=320, V=0)
D104 = units.BinaryDistillation('D104', D103-1, LHK=('Octene', 'Decene'),
k=1.05, y_top=0.98, x_bot=1e-6)
H107 = units.HXutility('H107', D104-0, T=320, V=0)
H108 = units.HXprocess('H108', (C103-0, D104-1), dT=5, phase1='l')
H108-0-D103
T108 = units.StorageTank('T108', H106-0, hexene,
vessel_type='Floating roof',
tau=7*24)
T109 = units.StorageTank('T109', H107-0, octene,
vessel_type='Floating roof',
tau=7*24)
T110 = units.StorageTank('T110', H108-1, decene,
vessel_type='Floating roof',
tau=7*24)
### Facilities ###
*other_agents, high_pressure_steam = bst.HeatUtility.heating_agents
BT = bst.BoilerTurbogenerator('BT',
ins=(None, None, 'boiler_makeup_water',
'natural_gas', 'lime', 'boiler_chemicals'),
boiler_efficiency = 0.80,
turbogenerator_efficiency=0.85,
agent=high_pressure_steam,
other_agents=other_agents)
CT = bst.CoolingTower('CT')
CWP = bst.ChilledWaterPackage('CWP')
CCI = bst.ChemicalCapitalInvestment('CCI', 'Tridecane', 644.05)
### System ###
sys = bst.System('LAOs_sys',
[bst.System('tridecane_recycle',
[fattyalcohol_production_sys,
bst.System('reaction_heat_integration_sys',
[H102,
H105,
T107,
M103,
H103,
R102],
recycle=R102-0),
P105,
C102,
P106,
bst.System('distillation_heat_integration_sys',
[H104,
D101,
D102,
C103,
H109,
M104,
M105,
P108],
recycle=P108-0),
P109],
recycle=1**F.unit.M101),
H108,
D103,
D104,
H106,
H107,
H108,
T108,
T109,
T110],
facilities=[CWP, BT, CT, BT, CCI])
if stainless_steel:
isa = isinstance
for i in sys.units:
if isa(i, bst.HX):
i.material = 'Stainless steel/stainless steel'
elif isa(i, bst.BinaryDistillation):
i.boiler.material = i.condenser.material = 'Stainless steel/stainless steel'
i.vessel_material = 'Stainless steel 304'
i.tray_material = 'Stainless steel 304'
elif isa(i, bst.Pump):
i.material = 'Stainless steel'
return sys
def create_wastewater_treatment_system(
wastewater_streams=(),
wastewater_treatment_area=600,
NaOH_price=0.15,
):
"""
Create a system for wastewater treatment.
Parameters
----------
wastewater_streams : Iterable[:class:`~thermosteam.Stream`], optional
Wastewater streams (without solids).
wastewater_treatment_area : int, optional
Area number to label unit operations. The default is 600.
NaOH_price : float, optional
Price of NaOH in USD/kg. The default is 0.15.
Returns
-------
wastewater_treatment : :class:`~biosteam.System`
Wastewater treatment system. The system includes anaerobic and aerobic
digestion, a membrane bioreactor, a sludge centrifuge, and reverse osmosis.
"""
n = wastewater_treatment_area
well_water = bst.Stream('well_water', Water=1, T=15 + 273.15)
air = bst.Stream('air_lagoon',
O2=51061,
N2=168162,
phase='g',
units='kg/hr')
caustic = bst.Stream('caustic',
Water=2252,
NaOH=2252,
units='kg/hr',
price=NaOH_price * 0.5)
wastewater_mixer = bst.Mixer(f'M{n+1}', wastewater_streams)
WWTC = WastewaterSystemCost('WWTC', wastewater_mixer - 0)
anaerobic_digestion = AnaerobicDigestion(f'R{n+1}', (WWTC - 0, well_water))
recycled_sludge_mixer = bst.Mixer(f'M{n+2}',
(anaerobic_digestion - 1, None))
caustic_over_waste = caustic.mol / 2544300.6261793654
air_over_waste = air.mol / 2544300.6261793654
waste = recycled_sludge_mixer - 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
aerobic_digestion = AerobicDigestion(f'R{n+2}', (waste, air, caustic),
outs=('evaporated_water', ''))
membrane_bioreactor = MembraneBioreactor(f'S{n+1}', aerobic_digestion - 1)
sludge_splitter = bst.Splitter(f'S{n+2}',
membrane_bioreactor - 1,
split=0.96)
fresh_sludge_mixer = bst.Mixer(
f'M{n+3}', (anaerobic_digestion - 2, sludge_splitter - 1))
sludge_centrifuge = SludgeCentrifuge(f'S{n+3}',
fresh_sludge_mixer - 0,
outs=('', 'sludge'))
sludge_centrifuge - 0 - 1 - recycled_sludge_mixer
reverse_osmosis = ReverseOsmosis(f'S{n+4}',
membrane_bioreactor - 0,
outs=('treated_water', 'waste_brine'))
aerobic_digestion_sys = bst.System(
'aerobic_digestion_sys',
path=(recycled_sludge_mixer, update_aerobic_input_streams,
aerobic_digestion, membrane_bioreactor, sludge_splitter,
fresh_sludge_mixer, sludge_centrifuge),
recycle=recycled_sludge_mixer - 0)
wastewater_treatment = bst.System('wastewater_treatment',
path=[
wastewater_mixer, WWTC,
anaerobic_digestion,
aerobic_digestion_sys,
reverse_osmosis
])
return wastewater_treatment
def create_system(ID='lipidcane_sys'):
chemicals = bst.settings.get_chemicals()
s = bst.main_flowsheet.stream
u = bst.main_flowsheet.unit
### Streams ###
lipidcane = lipidcane = bst.Stream('lipidcane',
Ash=2000.042,
Cellulose=26986.69,
Glucose=2007.067,
Hemicellulose=15922.734,
Lignin=14459.241,
Lipid=10035.334,
Solids=5017.667,
Sucrose=22746.761,
Water=234157.798,
units='kg/hr',
price=price['Lipid cane'])
enzyme = bst.Stream('enzyme',
Cellulose=100,
Water=900,
units='kg/hr',
price=price['Protease'])
imbibition_water = bst.Stream('imbibition_water',
Water=87023.35,
units='kg/hr',
T=338.15)
H3PO4 = bst.Stream('H3PO4',
H3PO4=74.23,
Water=13.10,
units='kg/hr',
price=price['H3PO4']) # to T203
lime = bst.Stream('lime',
CaO=333.00,
Water=2200.00,
units='kg/hr',
price=price['Lime']) # to P5
polymer = bst.Stream('polymer',
Flocculant=0.83,
units='kg/hr',
price=price['Polymer']) # to T205
rvf_wash_water = bst.Stream('rvf_wash_water',
Water=16770,
units='kg/hr',
T=363.15) # to C202
oil_wash_water = bst.Stream('oil_wash_water',
Water=1350,
units='kg/hr',
T=358.15) # to T207
### Unit operations ###
bst.Stream.ticket_name = 'd'
bst.Stream.ticket_number = 100
# Feed the shredder
U101 = units.ConveyingBelt('U101', ins=lipidcane)
U101.cost_items['Conveying belt'].ub = 5000
# Separate metals
U102 = units.MagneticSeparator('U102', ins=U101 - 0)
# Shredded cane
U103 = units.Shredder('U103', ins=U102 - 0)
bst.Stream.ticket_number = 200
# Hydrolyze starch
T201 = units.EnzymeTreatment('T201', T=323.15) # T=50
# Finely crush lipid cane
U201 = units.CrushingMill('U201',
split=dict(Ash=0.92,
Cellulose=0.92,
Glucose=0.04,
Hemicellulose=0.92,
Lignin=0.92,
Sucrose=0.04,
Lipid=0.1,
Solids=1),
moisture_content=0.5)
# Convey out bagasse
U202 = units.ConveyingBelt('U202', ins=U201.outs[0], outs='Bagasse')
# Mix in water
M201 = units.Mixer('M201')
# Screen out fibers
S201 = units.VibratingScreen('S201',
split=dict(Ash=0.35,
Cellulose=0.35,
Glucose=0.88,
Hemicellulose=0.35,
Lignin=0.35,
Lipid=0.88,
Solids=0,
Sucrose=0.88,
Water=0.88))
# Store juice before treatment
T202 = units.StorageTank('T202', tau=4, vessel_material='Carbon steel')
# Heat up before adding acid
H201 = units.HXutility('H201', T=343.15, V=0)
# Mix in acid
T203 = units.MixTank('T203')
T203.tau = 0.10
# Pump acid solution
P201 = units.Pump('P201')
# Mix lime solution
T204 = units.MixTank('T204')
T204.tau = 0.10
P202 = units.Pump('P202')
# Blend acid lipid solution with lime
T205 = units.MixTank('T205')
# Mix recycle
M202 = units.Mixer('M202')
# Heat before adding flocculant
H202 = units.HXutility('H202', T=372.15, V=0)
# Mix in flocculant
T206 = units.MixTank('T206')
T206.tau = 0.10
# Separate residual solids
C201 = units.Clarifier('C201',
split=dict(Ash=0,
CaO=0,
Cellulose=0,
Flocculant=0.522,
Glucose=0.522,
Hemicellulose=0,
Lignin=0,
Lipid=0.98,
H3PO4=0.522,
Sucrose=0.522,
Water=0.522))
# Remove solids as filter cake
C202 = units.RVF('C202',
outs=('filter_cake', ''),
moisture_content=0.80,
split=dict(Ash=0.85,
CaO=0.85,
Cellulose=0.85,
Glucose=0.01,
Hemicellulose=0.85,
Lignin=0.85,
Sucrose=0.01))
P203 = units.Pump('P203')
# Separate oil and sugar
T207 = units.MixTank('T207')
T207_2 = units.Splitter('T207_2', split=dict(Lipid=1, Water=1e-4))
# Cool the oil
H203 = units.HXutility('H203', T=343.15, V=0)
# Screen out small fibers from sugar stream
S202 = units.VibratingScreen('S202',
outs=('', 'fiber_fines'),
split=dict(Ash=1.0,
CaO=1.0,
Cellulose=1.0,
Flocculant=0.0,
Glucose=0.998,
Hemicellulose=1.0,
Lignin=1.0,
Lipid=1.0,
H3PO4=1.0,
Sucrose=0.998,
Water=0.998))
sugar = S202 - 0
S202.mesh_opening = 2
# Add distilled water to wash lipid
T208 = units.MixTank('T208')
T208.tau = 0.10
# Centrifuge out water
C203 = units.LiquidsSplitCentrifuge('C203',
split=dict(Lipid=0.99, Water=0.01))
# Vacume out water
F201 = units.SplitFlash('F201',
T=357.15,
P=2026.5,
outs=('water_vapor', ''),
split=dict(Lipid=0.0001, Water=0.999))
### Process specifications ###
def correct_flows():
F_mass = lipidcane.F_mass
# correct enzyme, lime, phosphoric acid, and imbibition water
enzyme.imass['Cellulose',
'Water'] = 0.003 * F_mass * np.array([0.1, 0.9])
lime.imass['CaO', 'Water'] = 0.001 * F_mass * np.array([0.046, 0.954])
H3PO4.imass['H3PO4', 'Water'] = 0.00025 * F_mass
imbibition_water.imass['Water'] = 0.25 * F_mass
T201._run()
T201.specification = correct_flows
# Specifications within a system
def correct_lipid_wash_water():
oil_wash_water.imol['Water'] = 100 / 11 * H202.outs[0].imol['Lipid']
T208._run()
T208.specification = correct_lipid_wash_water
def correct_wash_water():
P202._run()
solids = P202.outs[0].imol['Ash', 'CaO', 'Cellulose', 'Hemicellulose',
'Lignin'].sum()
rvf_wash_water.imol['Water'] = 0.0574 * solids
P202.specification = correct_wash_water
### System set-up ###
(U103 - 0, enzyme) - T201
(T201 - 0, M201 - 0) - U201 - 1 - S201 - 0 - T202
(S201 - 1, imbibition_water) - M201
T202 - 0 - H201
(H201 - 0, H3PO4) - T203 - P201
(P201 - 0, lime - T204 - 0) - T205 - P202
(P202 - 0, P203 - 0) - M202 - H202
(H202 - 0, polymer) - T206 - C201
(C201 - 1, rvf_wash_water) - C202 - 1 - P203
C201 - 0 - T207 - T207_2 - 0 - H203
(H203 - 0, oil_wash_water) - T208 - C203 - 0 - F201
T207 - T207_2 - 1 - S202
lipid = F201 - 1
### Ethanol section ###
### Utilities ###
MW_etoh = chemicals.Ethanol.MW
MW_water = chemicals.Water.MW
def mass2molar_ethanol_fraction(ethanol_mass_fraction):
"""Return ethanol mol fraction in a ethanol water mixture"""
x = ethanol_mass_fraction
return x / MW_etoh / (x / MW_etoh + (1 - x) / MW_water)
### Input streams ###
ethanol_production_sys = create_ethanol_production_system(
sugar_solution=S202 - 0)
u.M305.ins.append(C203 - 1)
### Biodiesel section ###
### Streams ###
# Fresh degummed oil
oil = lipid
# Fresh methanol
methanol = bst.Stream('methanol', Methanol=1, price=price['Methanol'])
# Catalyst
catalyst = bst.Stream('catalyst',
NaOCH3=0.25,
Methanol=0.75,
units='kg/hr',
price=price['NaOCH3'])
# price=0.25*price['NaOCH3'] + 0.75*Methanol.price)
# Water to remove glycerol
biodiesel_wash_water = bst.Stream('biodiesel_wash_water',
Water=13.6,
T=273.15 + 60,
price=price['Water'])
# Acid to neutralize catalyst after second centrifuge
HCl1 = bst.Stream('HCl1', HCl=0.21, Water=0.79, price=price['HCl'])
# price=0.21*price['HCl'] + 0.79*Water.price) # 35% HCl by mass
# Acid to remove soaps after first centrifuge
HCl2 = bst.Stream('HCl2', HCl=0.21, Water=0.79, price=HCl1.price)
# Base to neutralize acid before distillation
NaOH = bst.Stream('NaOH', NaOH=1, price=price['NaOH'])
# Products
crude_glycerol = bst.Stream('crude_glycerol',
price=price['Crude glycerol'])
biodiesel = bst.Stream('biodiesel', price=price['Biodiesel'])
# Waste
waste = bst.Stream('waste', price=price['Waste'])
### Units ###
### Biodiesel Transesterification Section ###
# Aparently reactors are adiabatic, meoh coming in at 40C, lipid at 60C
# From USDA Biodiesel model
x_cat = 1.05e-05 # Catalyst molar fraction in methanol feed
# Mix Recycle Methanol and Fresh Methanol
T401 = units.StorageTank('T401')
P401 = units.Pump('P401')
# Storage Tank for Catalyst
T402 = units.StorageTank('T402')
P402 = units.Pump('P402')
# Tank for oil
T403 = units.StorageTank('T403')
T403.tau = 4
P403 = units.Pump('P403')
# Mix Methanol and Catalyst stream
T404 = units.MixTank('T404')
P404 = units.Pump('P404')
# Split Methanol/Catalyst to reactors (this is done through a process specification, so use a fake splitter)
S401 = bst.FakeSplitter('S401')
# First Reactor
R401 = units.Transesterification('R401',
efficiency=0.90,
methanol2lipid=6,
T=333.15,
catalyst_molfrac=x_cat)
# Centrifuge to remove glycerol
C401 = units.LiquidsSplitCentrifuge('C401',
split=dict(Lipid=0.99,
Methanol=0.40,
Glycerol=0.06,
Biodiesel=0.999,
Water=0.40,
NaOH=0,
HCl=0,
NaOCH3=0.40))
P405 = units.Pump('P405')
# Second Reactor
R402 = units.Transesterification('R402',
efficiency=0.90,
methanol2lipid=6,
T=333.15,
catalyst_molfrac=x_cat)
def adjust_feed_to_reactors():
R402._run()
S401.ins[0].sum(S401.outs)
R402.specification = adjust_feed_to_reactors
# Centrifuge to remove glycerol
C402 = units.LiquidsSplitCentrifuge('C402',
split=dict(Lipid=0.90,
Methanol=0.10,
Glycerol=0.05,
Biodiesel=0.999,
Water=0.10,
NaOH=0,
HCl=0,
NaOCH3=0.10))
# Acids and bases per catalyst by mol
k1 = 0.323 / 1.5
k2 = 1.060 / 1.5
k3 = 0.04505 / 1.5
def adjust_acid_and_base():
T404._run()
# Adjust according to USDA biodiesel model
catalyst_mol = T404.outs[0].imol['NaOCH3']
NaOH.imol['NaOH'] = k1 * catalyst_mol
HCl1.imol['HCl'] = k2 * catalyst_mol
HCl2.imol['HCl'] = k3 * catalyst_mol
T404.specification = adjust_acid_and_base
### Biodiesel Purification Section ###
# Water wash
T405 = units.MixTank('T405')
P406 = units.Pump('P406')
# Centrifuge out water
C403 = units.LiquidsRatioCentrifuge('C403',
K_chemicals=('Methanol', 'Glycerol'),
Ks=np.array([0.382, 0.183]),
top_solvents=('Biodiesel', ),
top_split=(0.999, ),
bot_solvents=('Water', 'Lipid', 'NaOH',
'HCl'),
bot_split=(0.999, 1, 1, 1))
# Vacuum dry biodiesel
# Consider doing this by split, and keeping this unit constant
# 290 Pa, 324 K according to USDA Biodiesel Model
F401 = units.SplitFlash('F401',
order=('Water', 'Methanol', 'Biodiesel'),
split=(0.9999, 0.9999, 0.00001),
P=2026.5,
T=331.5,
Q=0)
F401.line = 'Vacuum dryer'
F401.material = 'Stainless steel 304'
P407 = units.Pump('P407')
### Glycerol Purification Section ###
# Condense vacuumed methanol to recycle
H401 = units.HXutility('H401', V=0, T=295)
P408 = units.Pump('P408')
# Mix recycled streams and HCl
T406 = units.MixTank('T406')
P409 = units.Pump('P409')
# Centrifuge out waste fat
# assume all the lipid, free_lipid and biodiesel is washed out
C404 = units.LiquidsSplitCentrifuge('C404',
outs=('', waste),
order=('Methanol', 'Glycerol',
'Water'),
split=(0.999, 0.999, 0.999))
# Add and mix NaOH
T407 = units.MixTank('T407')
P410 = units.Pump('P410')
# Methanol/Water distillation column
D401 = units.BinaryDistillation('D401',
LHK=('Methanol', 'Water'),
P=101325,
y_top=0.99999,
x_bot=0.0001,
k=2.5,
is_divided=True,
vessel_material='Stainless steel 304',
tray_material='Stainless steel 304')
# Condense water to recycle
H402 = units.HXutility('H402', T=353, V=0)
# Glycerol/Water flash (not a distillation column)
w = 0.20 / chemicals.Water.MW
g = 0.80 / chemicals.Glycerol.MW
x_water = w / (w + g)
D402 = units.BinaryDistillation('D402',
LHK=('Water', 'Glycerol'),
k=1.25,
P=101325,
y_top=0.999,
x_bot=x_water,
tray_material='Stainless steel 304',
vessel_material='Stainless steel 304')
def startup_water():
imol = D402.ins[0].imol
water, glycerol = imol['Water', 'Glycerol']
minimum_water = 5 * (w / (w + g)) * glycerol
if water < minimum_water:
imol['Water'] = minimum_water
D402._run()
# Remove accumulation
D402.outs[0].imol['Water'] = 1100 * C402.outs[0].imol['Glycerol']
D402.specification = startup_water
# Condense recycle methanol
H403 = units.HXutility('H403', V=0, T=315)
P411 = units.Pump('P411')
# Condense recycle water
H404 = units.HXutility('H404', V=0, T=315)
P412 = units.Pump('P412')
# Storage tank for glycerol
T408 = units.StorageTank('T408', outs=crude_glycerol)
# Storage tank for biodiesel
T409 = units.StorageTank('T409', outs=biodiesel)
F401 - 1 - P407 - 0 - T409
### Biodiesel system set-up ###
# Biodiesel Transesterification Section
oil - T403 - P403
(P403 - 0, S401 - 0) - R401 - 0 - C401
(C401 - 0, S401 - 1) - R402 - 0 - C402 - 1
# Specs for product https://www.afdc.energy.gov/fuels/biodiesel_specifications.html
# minimum spec requirements:
# 0.050 wt % water (lower to 0.045)
# 0.2 wt % meoh (lower to 0.15)
# 0.02 wt % glycerol (lower to 0.015)
# 0.4 wt % free lipids (lower to 0.35)
# Find Water Flow
def adjust_biodiesel_wash_water():
total_glycerol = (C401.outs[1].imol['Glycerol'] +
R402.outs[0].imol['Glycerol'])
wash_water = (x_water / (1 - x_water) * total_glycerol -
HCl1.imol['Water'] - NaOH.imol['Water'] -
oil.imol['Water'] - HCl2.imol['Water'])
biodiesel_wash_water.imol[
'Water'] = wash_water if wash_water > 0 else 0.
T405._run()
T405.specification = adjust_biodiesel_wash_water
D402 - 0 - H404 - 0 - P412
# Biodiesel wash
(C402 - 0, P412 - 0, biodiesel_wash_water, HCl1) - T405 - P406 - C403
# Glycerol recycle and purification section
C403 - 0 - F401
F401 - 0 - H401 - P408
C401 - 1 - P405
(P405 - 0, C402 - 1, C403 - 1, P408 - 0, HCl2) - T406 - P409 - C404
(C404 - 0, NaOH) - T407 - P410
H402 - 0 - D401 - 1 - D402 - 1 - T408
P410 - 0 - H402
# Mass Balance for Methanol, Recycle Methanol, and Catalyst stream
B401 = bst.MassBalance(
'B401',
description='Adjust catalyst and methanol feed to reactors',
variable_inlets=[catalyst, methanol],
constant_inlets=[D401 - 0],
constant_outlets=[1**R401, 1**R402],
chemical_IDs=('Methanol', 'NaOCH3'))
# Find Fresh Methanol Flow
D401 - 0 - B401 - H403 - P411 # Recycle methanol
methanol - T401 - P401 # Mix fresh and recycled methanol
catalyst - T402 - P402 # Fresh catalyst
(P411 - 0, P401 - 0,
P402 - 0) - T404 - P404 - S401 # Mix Catalyst with Methanol
# Initial guess
D402.outs[0].imol['Methanol', 'Glycerol',
'Water'] = [0.00127, 3.59e-05, 0.0244]
### Facilities ###
# Burn bagasse from conveyor belt
BT = units.BoilerTurbogenerator(
'BT', (U202 - 0, '', 'boiler_makeup_water', 'natural_gas', '', ''),
boiler_efficiency=0.80,
turbogenerator_efficiency=0.85)
CT = units.CoolingTower('CT')
makeup_water_streams = (s.cooling_tower_makeup_water,
s.boiler_makeup_water)
process_water_streams = (s.imbibition_water, s.biodiesel_wash_water,
oil_wash_water, rvf_wash_water, s.stripping_water,
*makeup_water_streams)
makeup_water = bst.Stream('makeup_water', price=0.000254)
CWP = units.ChilledWaterPackage('CWP')
PWC = units.ProcessWaterCenter('PWC', (bst.Stream(), makeup_water), (),
None, makeup_water_streams,
process_water_streams)
return bst.System(
ID,
[
U101, U102, U103, T201,
bst.System('juice_extraction_sys', [U201, S201, M201],
recycle=M201 - 0), T202, H201, T203, P201, T204, T205,
P202,
bst.System(
'juice_separation_sys', [M202, H202, T206, C201, C202, P203],
recycle=P203 - 0), T207, T207_2, H203, T208, C203, F201, T403,
P403, R401, C401, R402, C402,
bst.System('methanol_recycle_sys', [
T406, P409, C404, T407, P410, H402, D401, D402, H404, P412,
T405, P406, C403
],
recycle=C403 - 1), F401, P407, T409, H401, P408, P405,
B401, H403, P411, T401, P401, T402, P402, T404, P404, S401, S202,
ethanol_production_sys, T408, U202
],
facilities=(CWP, BT, CT, PWC),
)
