Hydrothermal

QSDsan: Quantitative Sustainable Design for sanitation and resource recovery systems

This module is developed by:

This module is under the University of Illinois/NCSA Open Source License. Please refer to https://github.com/QSD-Group/QSDsan/blob/main/LICENSE.txt for license details.

class qsdsan.unit_operations.static._hydrothermal.CatalyticHydrothermalGasification(ID='', ins: Sequence[AbstractStream] | None = None, outs: Sequence[AbstractStream] | None = (), thermo=None, init_with='Stream', pump_pressure=21302739.972, heat_temp=623.15, cool_temp=333.15, WHSV=3.562, catalyst_lifetime=7920, gas_composition={'C2H6': 0.011, 'C3H8': 0.03, 'CH4': 0.527, 'CO2': 0.432, 'H2': 0.0001}, gas_C_2_total_C=0.5981, P=None, tau=0.3333333333333333, void_fraction=0.5, length_to_diameter=2, diameter=None, N=6, V=None, auxiliary=False, mixing_intensity=None, kW_per_m3=0, wall_thickness_factor=1, vessel_material='Stainless steel 316', vessel_type='Vertical', CAPEX_factor=1)

CHG serves to reduce the COD content in the aqueous phase and produce fuel gas under elevated temperature (350°C) and pressure. The outlet will be cooled down and separated by a flash unit.

Parameters:

  • ins (Iterable(stream)) – chg_in, catalyst_in.

  • outs (Iterable(stream)) – chg_out, catalyst_out.

  • pump_pressure (float) – CHG influent pressure, [Pa].

  • heat_temp (float) – CHG influent temperature, [K].

  • cool_temp (float) – CHG effluent temperature, [K].

  • WHSV (float) – Weight Hourly Space velocity, [kg feed/hr/kg catalyst].

  • catalyst_lifetime (float) – CHG catalyst lifetime, [hr].

  • gas_composition (dict) – CHG gas composition.

  • gas_C_2_total_C (dict) – CHG gas carbon content to feed carbon content.

  • CAPEX_factor (float) – Factor used to adjust CAPEX.

References

[1] Jones, S. B.; Zhu, Y.; Anderson, D. B.; Hallen, R. T.; Elliott, D. C.;

Schmidt, A. J.; Albrecht, K. O.; Hart, T. R.; Butcher, M. G.; Drennan, C.; Snowden-Swan, L. J.; Davis, R.; Kinchin, C. Process Design and Economics for the Conversion of Algal Biomass to Hydrocarbons: Whole Algae Hydrothermal Liquefaction and Upgrading; PNNL–23227, 1126336; 2014; https://doi.org/10.2172/1126336.

[2] Davis, R. E.; Grundl, N. J.; Tao, L.; Biddy, M. J.; Tan, E. C.;

Beckham, G. T.; Humbird, D.; Thompson, D. N.; Roni, M. S. Process Design and Economics for the Conversion of Lignocellulosic Biomass to Hydrocarbon Fuels and Coproducts: 2018 Biochemical Design Case Update; Biochemical Deconstruction and Conversion of Biomass to Fuels and Products via Integrated Biorefinery Pathways; NREL/TP–5100-71949, 1483234; 2018; p NREL/TP–5100-71949, 1483234. https://doi.org/10.2172/1483234.

[3] Elliott, D. C.; Neuenschwander, G. G.; Hart, T. R.; Rotness, L. J.;

Zacher, A. H.; Santosa, D. M.; Valkenburg, C.; Jones, S. B.; Rahardjo, S. A. T. Catalytic Hydrothermal Gasification of Lignin-Rich Biorefinery Residues and Algae Final Report. 87.

auxiliary_unit_names: tuple[str, ...] = ('pump', 'heat_ex_heating', 'heat_ex_cooling')

Auxiliary unit operation names.

line: str = 'Catalytic hydrothermal gasification'

class-attribute Name denoting the type of Unit class. Defaults to the class name of the first child class

run()

Run mass and energy balance. This method also runs specifications user defined specifications unless it is being run within a specification (to avoid infinite loops).

See also

_run, specifications, add_specification, add_bounded_numerical_specification

class qsdsan.unit_operations.static._hydrothermal.HydrothermalLiquefaction(ID='', ins: Sequence[AbstractStream] | None = None, outs: Sequence[AbstractStream] | None = (), thermo=None, init_with='WasteStream', lipid_2_biocrude=0.846, protein_2_biocrude=0.445, carbo_2_biocrude=0.205, protein_2_gas=0.074, carbo_2_gas=0.418, biocrude_C_slope=-8.37, biocrude_C_intercept=68.55, biocrude_N_slope=0.133, biocrude_H_slope=-2.61, biocrude_H_intercept=8.2, HTLaqueous_C_slope=478, TOC_TC=0.764, hydrochar_C_slope=1.75, hydrochar_H_slope=0.141, biocrude_moisture_content=0.063, hydrochar_P_recovery_ratio=0.86, gas_composition={'C2H6': 0.032, 'CH4': 0.05, 'CO2': 0.918}, hydrochar_pre=20889054.371999998, HTLaqueous_pre=206842.80000000002, biocrude_pre=206842.80000000002, offgas_pre=206842.80000000002, eff_T=333.15, P=None, tau=0.25, V_wf=0.45, length_to_diameter=None, diameter=0.174625, N=4, V=None, auxiliary=False, mixing_intensity=None, kW_per_m3=0, wall_thickness_factor=1, vessel_material='Stainless steel 316', vessel_type='Horizontal', CAPEX_factor=1, HTL_steel_cost_factor=2.7, mositure_adjustment_exist_in_the_system=False)

HTL converts dewatered sludge to biocrude, aqueous, off-gas, and hydrochar under elevated temperature (350°C) and pressure. The products percentage (wt%) can be evaluated using revised MCA model (Li et al., 2017, Leow et al., 2018) with known sludge composition (protein%, lipid%, and carbohydrate%, all afdw%).

Notice that for HTL we just calculate each phases’ total mass (except gas) and calculate C, N, and P amount in each phase as properties. We don’t specify components for oil/char since we want to use MCA model to calculate C and N amount and it is not necessary to calculate every possible components since they will be treated in HT/AcidEx anyway. We also don’t specify components for aqueous since we want to calculate aqueous C, N, and P based on mass balance closure. But later for CHG, HT, and HC, we specify each components (except aqueous phase) for the application of flash, distillation column, and CHP units.

Parameters:

  • ins (Iterable(stream)) – dewatered_sludge.

  • outs (Iterable(stream)) – hydrochar, HTLaqueous, biocrude, offgas.

  • lipid_2_biocrude (float) – Lipid to biocrude factor.

  • protein_2_biocrude (float) – Protein to biocrude factor.

  • carbo_2_biocrude (float) – Carbohydrate to biocrude factor.

  • protein_2_gas (float) – Protein to gas factor.

  • carbo_2_gas (float) – Carbohydrate to gas factor.

  • biocrude_C_slope (float) – Biocrude carbon content slope.

  • biocrude_C_intercept (float) – Biocrude carbon content intercept.

  • biocrude_N_slope (float) – Biocrude nitrogen content slope.

  • biocrude_H_slope (float) – Biocrude hydrogen content slope.

  • biocrude_H_intercept (float) – Biocrude hydrogen content intercept.

  • HTLaqueous_C_slope (float) – HTLaqueous carbon content slope.

  • TOC_TC (float) – HTL TOC/TC.

  • hydrochar_C_slope (float) – Hydrochar carbon content slope.

  • hydrochar_H_slope (float) – Hydrochar hydrogen content slope.

  • biocrude_moisture_content (float) – Biocrude moisture content.

  • hydrochar_P_recovery_ratio (float) – Hydrochar phosphorus to total phosphorus ratio.

  • gas_composition (dict) – HTL offgas compositions.

  • hydrochar_pre (float) – Hydrochar pressure, [Pa].

  • HTLaqueous_pre (float) – HTL aqueous phase pressure, [Pa].

  • biocrude_pre (float) – Biocrude pressure, [Pa].

  • offgas_pre (float) – Offgas pressure, [Pa].

  • eff_T (float) – HTL effluent temperature, [K].

  • CAPEX_factor (float) – Factor used to adjust CAPEX.

  • HTL_steel_cost_factor (float) – Factor used to adjust the cost of stainless steel.

  • mositure_adjustment_exist_in_the_system (bool) – If a moisture adjustment unit exists, set to true.

References

[1] Leow, S.; Witter, J. R.; Vardon, D. R.; Sharma, B. K.;

Guest, J. S.; Strathmann, T. J. Prediction of Microalgae Hydrothermal Liquefaction Products from Feedstock Biochemical Composition. Green Chem. 2015, 17 (6), 3584–3599. https://doi.org/10.1039/C5GC00574D.

[2] Li, Y.; Leow, S.; Fedders, A. C.; Sharma, B. K.; Guest, J. S.;

Strathmann, T. J. Quantitative Multiphase Model for Hydrothermal Liquefaction of Algal Biomass. Green Chem. 2017, 19 (4), 1163–1174. https://doi.org/10.1039/C6GC03294J.

[3] Li, Y.; Tarpeh, W. A.; Nelson, K. L.; Strathmann, T. J.

Quantitative Evaluation of an Integrated System for Valorization of Wastewater Algae as Bio-Oil, Fuel Gas, and Fertilizer Products. Environ. Sci. Technol. 2018, 52 (21), 12717–12727. https://doi.org/10.1021/acs.est.8b04035.

[4] Jones, S. B.; Zhu, Y.; Anderson, D. B.; Hallen, R. T.; Elliott, D. C.;

Schmidt, A. J.; Albrecht, K. O.; Hart, T. R.; Butcher, M. G.; Drennan, C.; Snowden-Swan, L. J.; Davis, R.; Kinchin, C. Process Design and Economics for the Conversion of Algal Biomass to Hydrocarbons: Whole Algae Hydrothermal Liquefaction and Upgrading; PNNL–23227, 1126336; 2014; https://doi.org/10.2172/1126336.

[5] Matayeva, A.; Rasmussen, S. R.; Biller, P. Distribution of Nutrients and

Phosphorus Recovery in Hydrothermal Liquefaction of Waste Streams. BiomassBioenergy 2022, 156, 106323. https://doi.org/10.1016/j.biombioe.2021.106323.

[6] Knorr, D.; Lukas, J.; Schoen, P. Production of Advanced Biofuels

via Liquefaction - Hydrothermal Liquefaction Reactor Design: April 5, 2013; NREL/SR-5100-60462, 1111191; 2013; p NREL/SR-5100-60462, 1111191. https://doi.org/10.2172/1111191.

auxiliary_unit_names: tuple[str, ...] = ('heat_exchanger', 'kodrum')

Auxiliary unit operation names.

line: str = 'Hydrothermal liquefaction'

class-attribute Name denoting the type of Unit class. Defaults to the class name of the first child class

run()

Run mass and energy balance. This method also runs specifications user defined specifications unless it is being run within a specification (to avoid infinite loops).

See also

_run, specifications, add_specification, add_bounded_numerical_specification