# -*- coding: utf-8 -*-
# BioSTEAM: The Biorefinery Simulation and Techno-Economic Analysis Modules
# Copyright (C) 2020-2023, Yoel Cortes-Pena <yoelcortes@gmail.com>
#
# This module is under the UIUC open-source license. See
# github.com/BioSTEAMDevelopmentGroup/biosteam/blob/master/LICENSE.txt
# for license details.
"""
.. contents:: :local:
.. autoclass:: biosteam.units.single_phase_reactor.SinglePhaseReactor
References
----------
.. [1] Seider, W. D.; Lewin, D. R.; Seader, J. D.; Widagdo, S.; Gani, R.;
Ng, M. K. Product and Process Design Principles. Wiley 2017.
"""
from .abstract_stirred_tank_reactor import AbstractStirredTankReactor
__all__ = (
'SinglePhaseReactor',
)
[docs]
class SinglePhaseReactor(AbstractStirredTankReactor):
'''
Create a stirred tank reactor which assumes a single outlet stream with
no phase equilibrium.
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 0.985 [kW / m3] converted from
5 hp/1000 gal as in [1]_, for liquid–liquid reaction or extraction.
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
--------
Simulate the liquefaction of corn starch
(the enzymatic conversion of starch to glucose):
import biosteam as bst
from biorefineries import corn
chemicals = corn.create_chemicals()
bst.settings.set_thermo(chemicals)
feed = bst.Stream(
phase='l', T=360.15, P=1.555e+06,
Water=1.115e+05, Ethanol=0.1534,
Ash=647.3, Yeast=16.68, CaO=4.73,
TriOlein=1754, H2SO4=8.207, NH3=78.84,
Starch=2.83e+04, Fiber=5548,
SolubleProtein=1899, InsolubleProtein=2318,
units='kg/hr'
)
R1 = bst.SinglePhaseReactor(
ins=feed, outs='product',
reactions=bst.Reaction('Starch + H2O -> Glucose', 'Starch', 0.95),
heat_exchanger_configuration='jacketed',
tau=0.9, V_wf=0.90, V_max=500.,
kW_per_m3=0.6,
)
R1.simulate()
R1.show('cwt')
SinglePhaseReactor: R1
ins...
[0] feed
phase: 'l', T: 360.15 K, P: 1.555e+06 Pa
composition (%): Water 73.3
Ethanol 0.000101
Ash 0.426
Yeast 0.011
CaO 0.00311
TriOlein 1.15
H2SO4 0.0054
25.1
-------- 1.52e+05 kg/hr
outs...
[0] product
phase: 'l', T: 360.15 K, P: 1.555e+06 Pa
composition (%): Water 71.4
Ethanol 0.000101
Glucose 19.6
Ash 0.426
Yeast 0.011
CaO 0.00311
TriOlein 1.15
7.41
-------- 1.52e+05 kg/hr
R1.results()
Single phase reactor Units R1
Electricity Power kW 76.9
Cost USD/hr 6.02
Low pressure steam Duty kJ/hr 1.83e+06
Flow kmol/hr 47.4
Cost USD/hr 11.3
Design Reactor volume m3 142
Residence time hr 0.9
Vessel type Vertical
Length ft 38.6
Diameter ft 12.9
Weight lb 2.38e+05
Wall thickness in 1.62
Jacketed diameter 13.2
Vessel material Stainless steel 316
Purchase cost Vertical pressure vessel (jacketed) USD 4.09e+05
Platform and ladders USD 3.6e+04
Agitator - Agitator USD 5.77e+04
Total purchase cost USD 5.02e+05
Utility cost USD/hr 17.3
'''
_ins_size_is_fixed = False
_N_ins = _N_outs = 1
def _run(self):
ins = self.ins
effluent, = self.outs
if self.P is None: # Constant pressure
effluent.P = min([i.P for i in ins])
else:
effluent.P = self.P
if self.adiabatic:
Hnet = sum([i.Hnet for i in ins])
effluent.mix_from(ins, energy_balance=False)
self.reactions(effluent)
effluent.Hnet = Hnet
else:
if self.T is None:
effluent.mix_from(self.ins) # Constant temperature after mixing
else:
effluent.mix_from(self.ins, energy_balance=False)
effluent.T = self.T
self.reactions(effluent)
