single_phase_reactor#

class SinglePhaseReactor(ID='', ins=None, outs=(), thermo=None, **kwargs)[source]#

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

References

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