Hydroprocessing

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.sanunits._hydroprocessing.Hydrocracking(ID='', ins: Sequence[AbstractStream] | None = None, outs: Sequence[AbstractStream] | None = (), thermo=None, init_with='Stream', WHSV=0.625, catalyst_lifetime=39600, hydrogen_P=7168481.972000001, hydrogen_rxned_to_heavy_oil=0.01125, hydrogen_excess=5.556, hydrocarbon_ratio=1, HCin_T=667.15, HCrxn_T=724.15, HC_composition={'C10H22': 0.11756, 'C11H24': 0.16846, 'C12H26': 0.13198, 'C13H28': 0.09302, 'C14H30': 0.04643, 'C15H32': 0.0325, 'C16H34': 0.01923, 'C17H36': 0.00431, 'C18H38': 0.00099, 'C19H40': 0.00497, 'C20H42': 0.00033, 'C9H20': 0.09086, 'CH4': 0.0063, 'CO2': 0.0388, 'CYCHEX': 0.03714, 'HEPTANE': 0.11474, 'HEXANE': 0.01111, 'OCTANE': 0.08125}, P=None, tau=5, void_fraciton=0.4, length_to_diameter=2, diameter=None, N=None, V=None, auxiliary=False, mixing_intensity=None, kW_per_m3=0, wall_thickness_factor=1.5, vessel_material='Stainless steel 316', vessel_type='Vertical')

Biocrude mixed with H2 are hydrotreated at elevated temperature (405°C) and pressure to produce upgraded biooil. Co-product includes fuel gas.

Parameters:

  • ins (Iterable(stream)) – heavy_oil, hydrogen, catalyst_in.

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

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

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

  • hydrogen_P (float) – Hydrogen pressure, [Pa].

  • hydrogen_rxned_to_heavy_oil (float) – Reacted H2 to heavy oil mass ratio.

  • hydrogen_excess (float) – Actual hydrogen amount = hydrogen_rxned_to_biocrude*hydrogen_excess

  • hydrocarbon_ratio (float) – Mass ratio of produced hydrocarbon to the sum of heavy oil and reacted H2.

  • HCin_T (float) – HC influent temperature, [K].

  • HCrxn_T (float) – HC effluent (after reaction) temperature, [K].

  • HC_composition (dict) – HC effluent composition.

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.

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

class-attribute Name of attributes that are auxiliary units. These units will be accounted for in the purchase and installed equipment costs without having to add these costs in the baseline_purchase_costs dictionary. Heat and power utilities are also automatically accounted for.

line: str = 'Hydrocracking'

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

class qsdsan.sanunits._hydroprocessing.Hydrotreating(ID='', ins: Sequence[AbstractStream] | None = None, outs: Sequence[AbstractStream] | None = (), thermo=None, init_with='Stream', WHSV=0.625, catalyst_lifetime=15840, hydrogen_P=10548982.8, hydrogen_rxned_to_biocrude=0.046, hydrogen_excess=3, hydrocarbon_ratio=0.875, HTin_T=447.15, HTrxn_T=675.15, HT_composition={'C10H12': 0.0204, 'C10H16O4': 0.01837, 'C10H22': 0.0024, 'C11H24': 0.0204, 'C12H26': 0.0204, 'C15H32': 0.0612, 'C16H34': 0.1836, 'C17H36': 0.0816, 'C18H38': 0.0408, 'C19H40': 0.0408, 'C20H42': 0.102, 'C21H44': 0.0408, 'C24H38O4': 0.00817, 'C26H42O4': 0.0102, 'C2H6': 0.02923, 'C30H62': 0.00203, 'C3BENZ': 0.0102, 'C3H8': 0.0165, 'C4BENZ': 0.01223, 'C4H10': 0.0087, 'C6BENZ': 0.0204, 'C7BENZ': 0.0204, 'C8BENZ': 0.0204, 'C9H20': 0.00408, 'CC6METH': 0.0102, 'CH4': 0.0228, 'ETHCYC6': 0.00408, 'ETHYLBEN': 0.0204, 'FOURMONAN': 0, 'HEPTANE': 0.00401, 'HEXANE': 0.00401, 'NPENTAN': 0.00678, 'OCTANE': 0.01013, 'OTTFNA': 0.0102, 'OTTFSN': 0.0204, 'OXYLENE': 0.0102, 'PIPERDIN': 0.00408, 'PROCYC6': 0.00408, 'THREEMHEPTA': 0.0102, 'TOLUENE': 0.01013, 'TRICOSANE': 0.0408, 'TWOMBUTAN': 0.00408, 'TWOMHEXAN': 0.00408, 'TWOMPENTA': 0.00408}, P=None, tau=0.5, void_fraciton=0.4, length_to_diameter=2, diameter=None, N=None, 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, include_PSA=False, PSA_pre=4946300.824, PSA_efficiency=0.9)

Biocrude mixed with H2 are hydrotreated at elevated temperature (405°C) and pressure to produce upgraded biooil. Co-product includes fuel gas. A pressure swing adsorption (PSA) process can be optionally included for H2 recovery.

Parameters:

  • ins (Iterable(stream)) – biocrude, hydrogen, catalyst_in.

  • outs (Iterable(stream)) – ht_out, catalyst_out = self.outs.

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

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

  • hydrogen_P (float) – Hydrogen pressure, [Pa].

  • hydrogen_rxned_to_biocrude (float) – Reacted H2 to biocrude mass ratio.

  • hydrogen_excess (float) – Actual hydrogen amount = hydrogen_rxned_to_biocrude*hydrogen_excess

  • hydrocarbon_ratio (float) – Mass ratio of produced hydrocarbon to the sum of biocrude and reacted H2.

  • HTin_T (float) – HT influent temperature, [K].

  • HTrxn_T (float) – HT effluent (after reaction) temperature, [K].

  • HT_composition (dict) – HT effluent composition.

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

  • include_PSA (bool) – Whether to include pressure swing adsorption for H2 recovery.

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] Towler, G.; Sinnott, R. Chapter 14 - Design of Pressure Vessels.

In Chemical Engineering Design (Second Edition); Towler, G., Sinnott, R., Eds.; Butterworth-Heinemann: Boston, 2013; pp 563–629. https://doi.org/10.1016/B978-0-08-096659-5.00014-6.

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

class-attribute Name of attributes that are auxiliary units. These units will be accounted for in the purchase and installed equipment costs without having to add these costs in the baseline_purchase_costs dictionary. Heat and power utilities are also automatically accounted for.

line: str = 'Hydrotreating'

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