#################################################################################
# WaterTAP Copyright (c) 2020-2024, The Regents of the University of California,
# through Lawrence Berkeley National Laboratory, Oak Ridge National Laboratory,
# National Renewable Energy Laboratory, and National Energy Technology
# Laboratory (subject to receipt of any required approvals from the U.S. Dept.
# of Energy). All rights reserved.
#
# Please see the files COPYRIGHT.md and LICENSE.md for full copyright and license
# information, respectively. These files are also available online at the URL
# "https://github.com/watertap-org/watertap/"
#################################################################################
"""
This module contains a zero-order representation of a hydrothermal gasification unit.
"""
import pyomo.environ as pyo
from pyomo.environ import units as pyunits, Var
from idaes.core import declare_process_block_class
from watertap.core import build_sido_reactive, ZeroOrderBaseData
# Some more information about this module
__author__ = "Chenyu Wang"
[docs]@declare_process_block_class("HTGZO")
class HTGZOData(ZeroOrderBaseData):
"""
Zero-Order model for a hydrothermal gasification (HTG) unit.
"""
CONFIG = ZeroOrderBaseData.CONFIG()
[docs] def build(self):
super().build()
self._tech_type = "hydrothermal_gasification"
build_sido_reactive(self)
self.flow_mass_in = Var(
self.flowsheet().time,
units=pyunits.t / pyunits.hour,
bounds=(0, None),
doc="Inlet mass flowrate",
)
@self.Constraint(
self.flowsheet().time,
doc="Constraint for inlet mass flowrate.",
)
def cons_flow_mass(b, t):
return b.flow_mass_in[t] == pyunits.convert(
sum(
b.properties_in[t].flow_mass_comp[j]
for j in b.properties_in[t].component_list
),
to_units=pyunits.t / pyunits.hour,
)
self._perf_var_dict["Inlet Mass Flowrate"] = self.flow_mass_in
self.electricity = Var(
self.flowsheet().time,
units=pyunits.kW,
bounds=(0, None),
doc="Electricity consumption of unit",
)
self._perf_var_dict["Electricity Demand"] = self.electricity
self.energy_electric_flow_mass = Var(
units=pyunits.kWh / pyunits.t,
doc="Electricity intensity with respect to inlet flowrate",
)
@self.Constraint(
self.flowsheet().time,
doc="Constraint for electricity consumption based on inlet flowrate.",
)
def electricity_consumption(b, t):
return b.electricity[t] == pyunits.convert(
b.energy_electric_flow_mass * b.flow_mass_in[t], to_units=pyunits.kW
)
self._fixed_perf_vars.append(self.energy_electric_flow_mass)
self._perf_var_dict["Electricity Intensity"] = self.energy_electric_flow_mass
self.catalyst_dosage = Var(
units=pyunits.pound / pyunits.t,
bounds=(0, None),
doc="Dosage of catalyst per inlet flow",
)
self._fixed_perf_vars.append(self.catalyst_dosage)
self._perf_var_dict["Dosage of catalyst per inlet flow"] = self.catalyst_dosage
self.catalyst_flow = Var(
self.flowsheet().time,
units=pyunits.pound / pyunits.hr,
bounds=(0, None),
doc="Catalyst flow",
)
self._perf_var_dict["Catalyst flow"] = self.catalyst_flow
@self.Constraint(
self.flowsheet().time,
doc="Constraint for catalyst flow based on inlet flow rate.",
)
def eq_catalyst_flow(b, t):
return b.catalyst_flow[t] == pyunits.convert(
b.catalyst_dosage * b.flow_mass_in[t],
to_units=pyunits.pound / pyunits.hr,
)
@property
def default_costing_method(self):
return self.cost_hydrothermal_gasification
[docs] @staticmethod
def cost_hydrothermal_gasification(blk):
"""
General method for costing hydrothermal gasification unit. Capital cost
is based on the CHG reactor and other wastewater treatment equipment including
a feed pump, a booster pump, a feed/product exchanger, a fired heater,
a hydrocyclone, and a product air fin cooler.
"""
t0 = blk.flowsheet().time.first()
# Get parameter dict from database
parameter_dict = blk.unit_model.config.database.get_unit_operation_parameters(
blk.unit_model._tech_type, subtype=blk.unit_model.config.process_subtype
)
# Get costing parameter sub-block for this technology
(
IF_reactor,
EP_reactor,
F0_reactor,
SE_reactor,
IF_pump,
EP_pump,
F0_pump,
SE_pump,
IF_booster,
EP_booster,
F0_booster,
SE_booster,
IF_hydrocyclone,
EP_hydrocyclone,
F0_hydrocyclone,
SE_hydrocyclone,
IF_cooler,
EP_cooler,
F0_cooler,
SE_cooler,
IF_exchanger,
EP_exchanger,
F0_exchanger,
Fnew_exchanger,
SE_exchanger,
IF_heater,
EP_heater,
F0_heater,
Fnew_heater,
SE_heater,
) = blk.unit_model._get_tech_parameters(
blk,
parameter_dict,
blk.unit_model.config.process_subtype,
[
"installation_factor_reactor",
"equipment_cost_reactor",
"base_flowrate_reactor",
"scaling_exponent_reactor",
"installation_factor_pump",
"equipment_cost_pump",
"base_flowrate_pump",
"scaling_exponent_pump",
"installation_factor_booster",
"equipment_cost_booster",
"base_flowrate_booster",
"scaling_exponent_booster",
"installation_factor_hydrocyclone",
"equipment_cost_hydrocyclone",
"base_flowrate_hydrocyclone",
"scaling_exponent_hydrocyclone",
"installation_factor_cooler",
"equipment_cost_cooler",
"base_flowrate_cooler",
"scaling_exponent_cooler",
"installation_factor_exchanger",
"equipment_cost_exchanger",
"base_area_exchanger",
"new_area_exchanger",
"scaling_exponent_exchanger",
"installation_factor_heater",
"equipment_cost_heater",
"base_heat_duty_heater",
"new_heat_duty_heater",
"scaling_exponent_heater",
],
)
sizing_term_reactor = pyo.units.convert(
(blk.unit_model.flow_mass_in[t0] / F0_reactor),
to_units=pyo.units.dimensionless,
)
sizing_term_pump = pyo.units.convert(
(blk.unit_model.flow_mass_in[t0] / F0_pump),
to_units=pyo.units.dimensionless,
)
sizing_term_booster = pyo.units.convert(
(blk.unit_model.flow_mass_in[t0] / F0_booster),
to_units=pyo.units.dimensionless,
)
sizing_term_hydrocyclone = pyo.units.convert(
(blk.unit_model.flow_mass_in[t0] / F0_hydrocyclone),
to_units=pyo.units.dimensionless,
)
sizing_term_cooler = pyo.units.convert(
(blk.unit_model.flow_mass_in[t0] / F0_cooler),
to_units=pyo.units.dimensionless,
)
sizing_term_exchanger = pyo.units.convert(
(Fnew_exchanger / F0_exchanger),
to_units=pyo.units.dimensionless,
)
sizing_term_heater = pyo.units.convert(
(Fnew_heater / F0_heater),
to_units=pyo.units.dimensionless,
)
# Add cost variable and constraint
blk.capital_cost = pyo.Var(
initialize=1,
units=blk.config.flowsheet_costing_block.base_currency,
bounds=(0, None),
doc="Capital cost of unit operation",
)
reactor_cost = pyo.units.convert(
IF_reactor * EP_reactor * sizing_term_reactor**SE_reactor,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
pump_cost = pyo.units.convert(
IF_pump * EP_pump * sizing_term_pump**SE_pump,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
booster_cost = pyo.units.convert(
IF_booster * EP_booster * sizing_term_booster**SE_booster,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
hydrocyclone_cost = pyo.units.convert(
IF_hydrocyclone
* EP_hydrocyclone
* sizing_term_hydrocyclone**SE_hydrocyclone,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
cooler_cost = pyo.units.convert(
IF_cooler * EP_cooler * sizing_term_cooler**SE_cooler,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
exchanger_cost = pyo.units.convert(
IF_exchanger * EP_exchanger * sizing_term_exchanger**SE_exchanger,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
heater_cost = pyo.units.convert(
IF_heater * EP_heater * sizing_term_heater**SE_heater,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
expr = (
reactor_cost
+ pump_cost
+ booster_cost
+ hydrocyclone_cost
+ cooler_cost
+ exchanger_cost
+ heater_cost
)
blk.costing_package.add_cost_factor(
blk, parameter_dict["capital_cost"]["cost_factor"]
)
blk.capital_cost_constraint = pyo.Constraint(
expr=blk.capital_cost == blk.cost_factor * expr
)
# Register flows
blk.config.flowsheet_costing_block.cost_flow(
blk.unit_model.electricity[t0], "electricity"
)
blk.config.flowsheet_costing_block.cost_flow(
blk.unit_model.catalyst_flow[t0], "catalyst_HTG"
)