#################################################################################
# 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 membrane aerated biofilm reactor 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("MABRZO")
class MABRZOData(ZeroOrderBaseData):
"""
Zero-Order model for a MABR unit.
"""
CONFIG = ZeroOrderBaseData.CONFIG()
[docs] def build(self):
super().build()
self._tech_type = "mabr"
build_sido_reactive(self)
self.nitrogen_removal_rate = Var(
units=pyunits.g / pyunits.m**2 / pyunits.day,
bounds=(0, None),
doc="Nitrogen removal rate per day",
)
self._fixed_perf_vars.append(self.nitrogen_removal_rate)
self.reactor_area = Var(
units=pyunits.m**2,
bounds=(0, None),
doc="Sizing variable for effective reactor area",
)
@self.Constraint(
self.flowsheet().time,
doc="Constraint for effective reactor area",
)
def reactor_area_constraint(b, t):
return b.reactor_area == pyunits.convert(
b.properties_treated[t].flow_mass_comp["ammonium_as_nitrogen"]
/ b.nitrogen_removal_rate,
to_units=pyunits.m**2,
)
self._perf_var_dict["Reactor Area"] = self.reactor_area
self.air_flow_rate = Var(
self.flowsheet().config.time,
units=pyunits.m**3 / pyunits.hour / pyunits.m**2,
bounds=(0, None),
doc="Air flow rate per area",
)
self._fixed_perf_vars.append(self.air_flow_rate)
self.air_flow_vol = Var(
self.flowsheet().config.time,
units=pyunits.m**3 / pyunits.hour,
bounds=(0, None),
doc="Volumetric air flow rate",
)
@self.Constraint(
self.flowsheet().time,
doc="Constraint for air flow",
)
def air_flow_constraint(b, t):
return b.air_flow_vol[t] == pyunits.convert(
b.air_flow_rate[t] * b.reactor_area,
to_units=pyunits.m**3 / pyunits.hour,
)
self._perf_var_dict["Volumetric Air Flow Rate"] = self.air_flow_vol
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_vol_inlet = Var(
units=pyunits.kWh / pyunits.m**3,
doc="Electricity intensity with respect to inlet flowrate of unit",
)
@self.Constraint(
self.flowsheet().time,
doc="Constraint for electricity consumption based on air flowrate.",
)
def electricity_consumption(b, t):
return b.electricity[t] == (
b.energy_electric_flow_vol_inlet
* pyunits.convert(
b.air_flow_vol[t], to_units=pyunits.m**3 / pyunits.hour
)
)
self._fixed_perf_vars.append(self.energy_electric_flow_vol_inlet)
self._perf_var_dict["Electricity Intensity"] = (
self.energy_electric_flow_vol_inlet
)
@property
def default_costing_method(self):
return self.cost_mabr
[docs] @staticmethod
def cost_mabr(blk):
"""
General method for costing membrane aerated biofilm reactor. Capital cost
is based on the cost of reactor and blower.
This method also registers the electricity demand as a costed flow.
"""
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
A, B = blk.unit_model._get_tech_parameters(
blk,
parameter_dict,
blk.unit_model.config.process_subtype,
["reactor_cost", "blower_cost"],
)
# 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",
)
DCC_reactor = pyo.units.convert(
blk.unit_model.properties_treated[t0].flow_mass_comp["ammonium_as_nitrogen"]
/ blk.unit_model.nitrogen_removal_rate
* A,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
DCC_blower = pyo.units.convert(
blk.unit_model.reactor_area * blk.unit_model.air_flow_rate[t0] * B,
to_units=blk.config.flowsheet_costing_block.base_currency,
)
expr = DCC_reactor + DCC_blower
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"
)