Method and system for synthesizing fuel from dilute carbon dioxide source
A method for producing a synthetic fuel from hydrogen and carbon dioxide comprises extracting hydrogen molecules from hydrogen compounds in a hydrogen feedstock to produce a hydrogen-containing fluid stream; extracting carbon dioxide molecules from a dilute gaseous mixture in a carbon dioxide feedstock to produce a carbon dioxide containing fluid stream; and processing the hydrogen and carbon dioxide containing fluid streams to produce a synthetic fuel. At least some thermal energy and/or material used for at least one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams is obtained from thermal energy and/or material produced by another one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams.
1. A system for producing a liquid synthetic fuel from carbon dioxide, comprising:
a carbon dioxide capture subsystem configured to extract carbon dioxide molecules from a dilute gaseous mixture in an atmospheric carbon dioxide feedstock to produce a carbon-dioxide containing feed stream, the carbon dioxide capture subsystem comprising:
a gas-liquid contactor configured to flow a carbon dioxide capture solution; and
a calciner configured to produce a calciner gaseous product stream comprising the carbon-dioxide containing feed stream; and
a hydrocarbon production subsystem coupled to the carbon dioxide capture subsystem, the hydrocarbon production subsystem comprising a syngas generation reactor (SGR) unit configured to react the carbon-dioxide containing feed stream and a hydrogen-containing feed stream, the hydrocarbon production subsystem configured to produce the liquid synthetic fuel.
2. The system of claim 1 , further comprising a hydrogen production subsystem comprising an electrolyzer configured to produce an oxygen stream to flow through an oxidant conduit that fluidly couples the electrolyzer with at least one of the carbon dioxide capture subsystem or with the hydrocarbon production subsystem.
3. The system of claim 1 , further comprising a water conduit that fluidly couples a hydrogen production subsystem configured to produce the hydrogen- containing feed stream and the SGR unit, the water conduit configured to flow water produced by the SGR unit to the hydrogen production subsystem.
4. The system of claim 1 , further comprising a fuel conduit that couples the calciner of the carbon dioxide capture subsystem to the hydrocarbon production subsystem.
5. The system of claim 1 , further comprising:
a high temperature solids removal unit;
a water conduit that couples the high temperature solids removal unit to a hydrogen production subsystem; and
a calciner product conduit that couples the calciner and the high temperature solids removal unit.
6. The system of claim 1 , further comprising:
a high temperature solids removal unit;
a product conduit that couples the high temperature solids removal unit to a hydrogen production subsystem; and
a calciner product conduit that couples the calciner and the high temperature solids removal unit.
7. The system of claim 1 , wherein the carbon dioxide capture subsystem comprises:
a solution processing unit; and
an air contactor configured to flow the carbon dioxide capture solution to the solution processing unit, the carbon dioxide capture solution being thermally coupled to the hydrocarbon production subsystem such that heat is transferable from the hydrocarbon production subsystem to the carbon dioxide capture solution.
8. The system of claim 1 , wherein:
the hydrocarbon production subsystem comprises a Fischer Tropsch (FT) unit; and
at least one of the FT unit or the SGR unit is fluidly coupled to the carbon dioxide capture subsystem with a water conduit.
9. The system of claim 1 , wherein:
the SGR unit has an operating pressure selected to enable the SGR unit to receive the carbon-dioxide containing feed stream without being substantially cooled and compressed between the calciner and the SGR unit;
the operating pressure of the SGR unit is between 1-10 bar; and
the carbon-dioxide containing feed stream configured to be received at the SGR unit at a temperature between 850-900 Celsius.
10. The system of claim 1 , wherein the SGR unit comprises one or more reactant inlets configured to receive one or more SGR reactant feed streams, the one or more SGR reactant feed streams comprising at least one of a carbon dioxide reactant feed stream, a hydrogen reactant feed stream, a methane reactant feed stream, a water reactant feed stream, or a FT light end hydrocarbon reactant feed stream.
11. The system of claim 10 , wherein the carbon dioxide reactant feed stream comprises at least some of the carbon-dioxide containing feed stream.
12. The system of claim 10 , wherein the hydrocarbon production subsystem further comprises a syngas treatment unit configured to receive a syngas stream from the SGR unit and to discharge one or more recycle streams, wherein the one or more recycle streams comprise at least one of the water reactant feed stream, the hydrogen reactant feed stream, or the carbon dioxide reactant feed stream.
13. The system of claim 12 , further comprising at least one electric heater thermally coupled to one or more of the one or more recycle streams or the one or more SGR reactant feed streams, the electric heater comprising at least one of an inline electric heater, electrical heating tape, resistance heating wire, coils, or elements.
14. The system of claim 1 , wherein the SGR unit comprises an SGR burner thermally coupled to an SGR vessel, the SGR burner comprising a fuel inlet configured to receive the hydrogen-containing feed stream as fuel for combustion.
15. The system of claim 1 , wherein the calciner comprises an electric heating element or a calciner burner thermally coupled to at least one of a fluidized bed reactor vessel or a kiln reactor vessel.
16. The system of claim 1 , wherein the calciner comprises a calciner burner thermally coupled to a calciner reactor vessel, the calciner burner comprising a fuel inlet configured to receive at least some of the hydrogen-containing feed stream.
17. The system of claim 1 , wherein the SGR unit comprises an SGR burner and the calciner comprises a calciner burner, the SGR burner and the calciner burner each comprising a respective fuel inlet, wherein the respective fuel inlet of at least one of the SGR burner or the calciner is configured to receive one or more of a natural gas stream and a FT light end hydrocarbon stream from the hydrocarbon production subsystem.
18. The system of claim 1 , wherein at least one of the carbon dioxide capture subsystem, a hydrogen production subsystem, or the hydrocarbon production subsystem is thermally coupled to at least another one of the subsystems such that at least some thermal energy produced by one subsystem is transferrable to at least another one of the subsystems.
19. The system of claim 1 , wherein at least one of the carbon dioxide capture subsystem, a hydrogen production subsystem, or the hydrocarbon production subsystem is physically coupled to at least another one of the subsystems by a material transfer coupling configured to transfer at least some material produced in one subsystem to at least another one of the subsystems.