# -*- coding: utf-8 -*-
"""
.. contents:: :local:
.. autoclass:: biosteam.units.anaerobic_bioreactor.AnaerobicBioreactor
References
----------
.. [1] Benz, G. T. Optimize Power Consumption in Aerobic Fermenters.
Chem. Eng. Progress 2003, 99 (5), 100–103.
.. [2] Benz, G. T. Bioreactor Design for Chemical Engineers. Chem. Eng.\
Progress 2011, 21–26.
.. [3] Seider, W. D., Lewin, D. R., Seader, J. D., Widagdo, S., Gani, R.,
& Ng, M. K. (2017). Product and Process Design Principles. Wiley.
"""
import biosteam as bst
from .abstract_stirred_tank_reactor import AbstractStirredTankReactor
from .design_tools.aeration import vent_broth
__all__ = (
'AnaerobicBioreactor', 'AnBR',
)
[docs]
class AnaerobicBioreactor(AbstractStirredTankReactor):
"""
Create an anaerobic bioreactor with a vented stream and an effluent stream.
The reactor is designed as a pressure vessel with a given aspect ratio and
residence time. A pump-heat exchanger recirculation loop can be used to satisfy
the duty, if any. By default, a turbine agitator is also included if the
power usage, `kW_per_m3`, is positive. A vacuum system is also
automatically added if the operating pressure is at a vacuum.
Parameters
----------
tau :
Residence time [hr].
T :
Operating temperature [K].
P :
Operating pressure [Pa].
V_wf :
Fraction of working volume over total volume. Defaults to 0.8.
length_to_diameter :
Length to diameter ratio of bioreactor.
V_max :
Maximum volume of a reactor [m3]. Defaults to 355.
kW_per_m3 :
Power usage of agitator. Defaults to 0.2955 [kW / m3] from [1]_.
vessel_material :
Vessel material. Defaults to 'Stainless steel 316'.
vessel_type :
Vessel type. Valid options are 'Horizontal' or 'Vertical'. Defaults to 'Vertical'
batch :
Whether to use batch operation mode. If False, operation mode is continuous.
Defaults to `continuous`.
tau_0 :
Cleaning and unloading time (if batch mode). Defaults to 3 hr.
N :
Number of reactors.
heat_exchanger_configuration :
What kind of heat exchanger to default to (if any). Valid options include
'jacketed', 'recirculation loop', and 'internal coil'. Defaults to 'recirculation loop'.
dT_hx_loop :
Maximum change in temperature for the heat exchanger loop. Defaults to 5 K.
jacket_annular_diameter :
Annular diameter of heat exchanger jacket to vessel [m]. Defaults to 0.1 m.
loading_time :
Loading time of batch reactor. If not given, it will assume each vessel is constantly
being filled.
Notes
-----
The heat exchanger configuration can be one of the following:
* 'recirculation loop':
The recirculation loop takes into account the required flow rate needed to
reach the maximum temperature change of the heat exchanger, `dT_hx_loop`.
Increasing `dT_hx_loop` decreases the required recirculation flow rate and
therefore decreases pump costs.
When parallel reactors are required, one recirculation loop (each with a
pump and heat exchanger) is assumed. Although it is possible to use the
same recirculation loop for all reactors, this conservative assumption allows
for each reactor to be operated independently from each other.
* 'jacketed':
The jacket does not account for the heat transfer area requirement.
It simply assumes that a full jacket can provide the necessary heat transfer
area to meet the duty requirement. A heuristic annular diameter is assumed
through `jacket_annular_diameter` (which can be adjusted by the user).
The temperature at the wall is assumed to be the operating temperature.
The weight of the jacket is added to the weight of the vessel and the
cost is compounded together as a jacketed vessel.
* 'internal coil':
The internal coil is costed as an ordinary helical tube heat exchanger
with the added assumption that the temperature at the wall is the
operating temperature. This method is still not implemented in BioSTEAM
yet.
Examples
--------
>>> from biorefineries.cane import create_sugarcane_chemicals
>>> from biosteam import AnaerobicBioreactor, ReactionSystem, Reaction, Stream, settings
>>> settings.set_thermo(create_sugarcane_chemicals())
>>> feed = Stream(Water=1.20e+05,
... Glucose=1.89e+03,
... Sucrose=2.14e+04,
... DryYeast=1.03e+04,
... units='kg/hr',
... T=32+273.15)
>>> F1 = AnaerobicBioreactor(
... ins=feed, outs=('CO2', 'product'),
... tau=8, heat_exchanger_configuration='jacketed', batch=False,
... reactions=ReactionSystem(
... Reaction('Sucrose + Water -> 2Glucose', 'Sucrose', 1.0), # Hydrolysis
... Reaction('Glucose -> 2Ethanol + 2CO2', 'Glucose', 0.9), # Production
... Reaction('Glucose -> Yeast', 'Glucose', 0.70, basis='wt'), # Growth
... basis='mol',
... )
... )
>>> F1.simulate()
>>> F1.show()
AnaerobicBioreactor: R3
ins...
[0] s10
phase: 'l', T: 305.15 K, P: 101325 Pa
flow (kmol/hr): Water 6.66e+03
Glucose 10.5
Sucrose 62.5
Yeast 456
outs...
[0] CO2
phase: 'g', T: 305.15 K, P: 101325 Pa
flow (kmol/hr): Water 11.8
Ethanol 4.35
CO2 244
[1] product
phase: 'l', T: 305.15 K, P: 101325 Pa
flow (kmol/hr): Water 6.59e+03
Ethanol 240
Glucose 4.07
Yeast 532
>>> F1.results()
Anaerobic bioreactor Units R3
Electricity Power kW 10.2
Cost USD/hr 0.798
Chilled water Duty kJ/hr -1.4e+07
Flow kmol/hr 9.35e+03
Cost USD/hr 69.8
Design Reactor volume m3 1.28e+03
Number of reactors 1
Residence time hr 8
Vessel type Vertical
Length ft 80.2
Diameter ft 26.7
Weight lb 3.35e+05
Wall thickness in 0.508
Jacketed diameter ft 27.1
Vessel material Stainless steel 316
Purchase cost Vertical pressure vessel (jacketed) USD 5.3e+05
Platform and ladders USD 1.03e+05
Agitator - Agitator USD 1.83e+04
Total purchase cost USD 6.52e+05
Installed equipment cost USD 2.33e+06
Utility cost USD/hr 70.5
"""
_N_ins = 1
_N_outs = 2
_ins_size_is_fixed = False
T_default = 273.15 + 32
P_default = 101325
jacket_annular_diameter_default = 0.1 # [m]
V_max_default = 3785 # 1 million gallon is not unheard of for anaerobic bioreactors
kW_per_m3_default = 0.01 # Significantly less than aerobic, based on NREL 2011 report on cellulosic ethanol production.
batch_default = True
def _get_duty(self):
return self.Hnet
@property
def feed(self):
return self._ins[0]
@property
def vent(self):
return self._outs[0]
def _run_vent(self, vent, effluent):
vent_broth(vent, effluent)
def _run(self):
vent, effluent = self.outs
effluent.mix_from(self.ins)
self.reactions(effluent)
for i in self.outs:
i.T = self.T
i.P = self.P
vent.empty()
self._run_vent(vent, effluent)
AnBR = AnaerobicBioreactor
