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WO2025230511A1 - Système et procédé de capture directe d'air à l'aide de chaleur perdue - Google Patents

Système et procédé de capture directe d'air à l'aide de chaleur perdue

Info

Publication number
WO2025230511A1
WO2025230511A1 PCT/US2024/026883 US2024026883W WO2025230511A1 WO 2025230511 A1 WO2025230511 A1 WO 2025230511A1 US 2024026883 W US2024026883 W US 2024026883W WO 2025230511 A1 WO2025230511 A1 WO 2025230511A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluid
gas
heat
thermal
working fluid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/US2024/026883
Other languages
English (en)
Inventor
Dhinesh THANGANADAR
Todd Andrew Jankowski
William Dwight Gerstler
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ge Vernova Technology GmbH
GE Vernova Infrastructure Technology LLC
Original Assignee
Ge Vernova Technology GmbH
GE Vernova Infrastructure Technology LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ge Vernova Technology GmbH, GE Vernova Infrastructure Technology LLC filed Critical Ge Vernova Technology GmbH
Priority to PCT/US2024/026883 priority Critical patent/WO2025230511A1/fr
Publication of WO2025230511A1 publication Critical patent/WO2025230511A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/14—Power generation using energy from the expansion of the refrigerant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B27/00—Machines, plants or systems, using particular sources of energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/06—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using expanders

Definitions

  • the present application relates generally to a system and method for capturing undesirable gases from air or other gases.
  • the atmosphere contains air and various undesirable gases.
  • the undesirable gases may include carbon oxides (COx) such as carbon dioxide (CO2) and carbon monoxide (CO), nitrogen oxides (NOx) such as nitrogen dioxide (NO2), and/or sulfur oxides (SOx) such as sulfur dioxide (SO2).
  • CO2 is both an acid gas and a greenhouse gas.
  • ppmv parts per million by volume
  • ppmw parts per million by weight
  • a system includes a direct air capture (DAC) system, including one or more gas capture systems configured to capture an undesirable gas from air.
  • the system further includes a thermodynamic cycle including a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid
  • the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid
  • the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • a system includes a controller having memory, a processor, and instructions stored on the memory and executable by the processor to control a direct air capture (DAC) system including one or more gas capture systems to capture an undesirable gas from air.
  • the processor of the controller is further configured to control a thermodynamic cycle to provide heat to the one or more gas capture systems.
  • the thermodynamic cycle includes a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid
  • the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid
  • the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • a method includes controlling a direct air capture (DAC) system including one or more gas capture systems to capture an undesirable gas from air.
  • the method further includes controlling a thermodynamic cycle to provide heat to the one or more gas capture systems.
  • the thermodynamic cycle includes a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid
  • the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid
  • the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • FIG. 1 is a block diagram of an embodiment of a combined cycle system having a heat source, a steam generation system, a steam turbine system, a direct air capture (DAC) system having one or more gas capture systems, and a waste heat recovery system having a thermodynamic cycle and a thermal storage system configured to provide a thermal fluid to the gas capture systems.
  • DAC direct air capture
  • FIG. 2 is a schematic of an embodiment of a gas capture system of FIG. 1. illustrating a sorbent-based gas capture system having an adsorption mode, a desorption mode, and a cooling mode, wherein the waste heat recovery system provides the thermal fluid for the desorption mode.
  • FIG. 3 is a schematic of an embodiment of a gas capture system of FIG. 1, illustrating a solvent-based gas capture system having an absorber and a stripper, wherein the waste heat recovery system provides the thermal fluid for the stripper.
  • FIG. 4 is a schematic of an embodiment of the combined cycle system of FIG. 1, illustrating an embodiment of the thermodynamic cycle of the waste heat recovery system.
  • FIG. 5 is a schematic of an embodiment of the combined cycle system of FIG. 1, illustrating an embodiment of the thermodynamic cycle of the waste heat recovery system.
  • FIG. 6 is a schematic of an embodiment of the combined cycle system of FIG. 1, illustrating an embodiment of the thermodynamic cycle of the waste heat recovery 7 system.
  • the disclosed embodiments include systems and methods to reduce the undesirable gases in the atmosphere using a direct air capture (DAC) system having one or more gas capture systems.
  • the gas capture systems are configured to remove undesirable gases (e.g., CO2) from the air or any other gases.
  • the gas capture systems may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or a combination thereof.
  • the gas capture systems (e.g.. sorbent-based gas capture systems) may include one or more temperature swing adsorption (TSA) systems, vacuum temperature swing adsorption (VTSA) systems, concentration swing adsorption (CSA) systems, or any combination thereof.
  • TSA temperature swing adsorption
  • VTSA vacuum temperature swing adsorption
  • CSA concentration swing adsorption
  • the gas capture systems may include one or more temperature swing adsorption (TSA) units or adsorbers, which rely on temperature swings to adsorb undesirable gases at a first temperature (e.g., low temperature) and desorb the undesirable gases at a second temperature (e.g., high temperature).
  • TSA temperature swing adsorption
  • the gas capture systems may include one or more vacuum temperature swing adsorption (VTSA) units or adsorbers, which rely on temperature and pressure swings to adsorb undesirable gases at a first temperature (e.g., low temperature) and a first pressure (e.g., high pressure) and desorb the undesirable gases at a second temperature (e.g., high temperature) and a second pressure (e.g., low pressure).
  • VTSA vacuum temperature swing adsorption
  • a heat source to facilitate the desorption may include a variety of heated fluids, such as steam, an inert gas (e.g., nitrogen (N2)), or any other suitable sweep gas.
  • thermodynamic cycles configured to receive heat from one or more heat sources (e.g., nuclear reactor, combustion system, and/or solar thermal system) and produce electrical power may also be configured with waste heat recovery (WHR) systems to provide otherwise wasted heat to the gas capture process, thereby helping to reduce the overall operating cost of the gas capture process.
  • the system may include a thermodynamic cycle (e.g., Brayton cycle), which may be configured to provide waste heat through WHR to the gas capture system.
  • the thermodynamic cycle may use a working fluid, such as one or more of a supercritical fluid, an inert gas such as a noble gas, an organic working fluid, or any combination thereof, as discussed in further detail below.
  • the use of waste heat to support the gas capture process helps to reduce overall gas capture costs, thereby helping to facilitate commercialization of the gas capture system.
  • the sorbent-based gas capture systems are configured to adsorb the undesirable gases into a sorbent material, and then subsequently desorb the undesirable gases from the sorbent material using a heat source (e.g., a heated fluid).
  • a heat source e.g., a heated fluid
  • the adsorption process is exothermic, while the desorption process is endothermic.
  • the thermodynamic cycle of the WHR system is coupled to the sorbent-based gas capture system (e.g., desorption mode, stage, or section) as the heat source, thereby providing heat (e.g., heated fluid) to facilitate the desorption process.
  • the thermodynamic cycle of the WHR system may substantially reduce or eliminate the need for other heat sources to support the desorption process.
  • the solvent-based gas capture systems may include an absorber configured to absorb the undesirable gas into a solvent, and a stripper configured to strip the undesirable gas from the solvent using a heat source (e.g., a heated fluid).
  • a heat source e.g., a heated fluid
  • the solvent-based gas capture systems are discussed as using a solvent as an absorbent fluid, the disclosed embodiments may use any suitable absorbent fluid for capturing undesirable gases. Accordingly, the solvent-based gas capture system also may be described as a fluid absorbent-based gas capture system.
  • the thermodynamic cycle of the WHR system is coupled to the solventbased gas capture system (e.g., stripper) as the heat source, thereby providing heat (e.g.. heated fluid) to facilitate the desorption process.
  • the thermodynamic cycle of the WHR system may substantially reduce or eliminate the need for other heat sources to support the desorption process.
  • thermodynamic cycle of the WHR system may be used in a variety of configurations with the gas capture systems. Although specific examples are provide below, the thermodynamic cycle of the WHR system may be used in any suitable manner to support various gas capture systems, including but not limited to, sorbent-based gas capture systems, solvent-based gas capture systems, and cryogenic gas capture systems.
  • FIG. 1 is a block diagram of an embodiment of a combined cycle system 10 having a power system 12.
  • a steam turbine system 14 a steam generation system 16, a direct air capture (DAC) system 18 having one or more gas capture systems 20, and a waste heat recovery (WHR) system 22 coupled to and/or including a thermodynamic cycle 24 (e.g., Brayton cycle).
  • the power system 12 includes a heat source 26 having a plurality of thermal power systems 28 configured to provide heat to drive the steam generation system 16 and the thermodynamic cycle 24.
  • the steam generation system 16 uses the heat to generate steam to power one or more steam turbine systems 14, which in turn drive one or more loads 100 (e.g., mechanical loads and/or electrical generators).
  • loads 100 e.g., mechanical loads and/or electrical generators.
  • the heat drives operation of the thermodynamic cycle 24, which in turn drives one or more loads 25 (e.g., mechanical loads and/or electrical generators).
  • loads 25 e.g., mechanical loads and/or electrical generators
  • the power system 12, the steam turbine system 14, the steam generation system 16, and the thermodynamic cycle 24 may collectively operate to generate electricity, such as for an electrical power grid.
  • the thermodynamic cycle 24 may provide waste heat to one or more gas capture systems 20 of the DAC system 18 via the WHR system 22.
  • the waste heat of the thermodynamic cycle 24 would otherwise not be used by the thermodynamic cycle 24 and would be discharged to the environment.
  • the WHR system 22 uses the waste heat of the thermodynamic cycle 22 as a heat source for the DAC system 18, thereby helping to reduce costs associated with operating the DAC system 18.
  • the one or more gas capture systems 20 of the DAC system 18 are configured to capture an undesirable gas (e.g., CO2) from a gas, such as air.
  • the gas capture systems 20 may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof.
  • the WHR system 22 uses heat (e.g., waste heat such as a thermal fluid 30) from the power system 12 to heat a working fluid 32 of the thermodynamic cycle 24, which in turn provides heat (e.g., waste heat such as a thermal fluid 34) to operate the one or more gas capture systems 20 of the DAC system 18.
  • the thermodynamic cycle 24 may include one or more heat exchangers (e.g., recuperators or coolers) configured to transfer heat from the thermal fluid 30 to the working fluid 32 and one or more heat exchangers configured to transfer heat from the working fluid 32 to the thermal fluid 34.
  • the thermodynamic cycle 24 e.g., Brayton cycle
  • the thermodynamic cycle 24 also may be described as a thermodynamic cycle system (e.g., Brayton cycle system), such as a thermodynamic power cycle system or a thermodynamic heat pump cycle system.
  • the working fluid 32 includes one or more of a supercritical fluid (SCF), an inert gas such as a noble gas, an organic working fluid, or any combination thereof. Additionally, in certain embodiments, the working fluid 32 excludes a combustion gas (e.g., exhaust gas, flue gas), and the thermodynamic cycle 24 excludes a combustion system providing the combustion gas as the working fluid 32. Instead, the thermodynamic cycle 24 relies on waste heat from the heat source 26.
  • the thermal fluid 34 may be configured to transfer heat to the one or more gas capture systems 20 to enable or improve desorption of the undesirable gas (e.g., CO2) during a desorption mode.
  • the undesirable gas e.g., CO2
  • the power system 12 includes the heat source 26 having the plurality 7 of thermal power systems 28 configured to provide heat to the steam generation system 16.
  • the thermal power systems 28 include a nuclear system 50 (e.g.. nuclear reactor system), a combustion system 52. and a solar thermal system 54.
  • the steam generation system 16 includes steam generators 56, 58, and 60.
  • the nuclear system 50 may include a nuclear reactor or reactor core configured to initiate and control a fission nuclear chain reaction or nuclear fusion reactions, thereby providing heat to the steam generator 56 to generate a steam 62.
  • the combustion system 52 may include a furnace or combustion vessel configured to combust a fuel (e.g., coal, biofuel, liquid fuel, gas fuel, etc.) to generate hot combustion gases, which in turn provide heat to the steam generator 58 to generate a steam 64.
  • the solar thermal system 54 may include a plurality 7 of solar thermal collectors configured to harness solar energy to provide heat to the steam generator 60 to generate a steam 66.
  • the steam 62, 64, and 66 provided by the respective steam generators 56, 58, and 60 may include one or more steam flows of a high-pressure steam (HP steam), an intermediate-pressure (IP) steam, a low-pressure (LP) steam, or a combination thereof.
  • HP steam high-pressure steam
  • IP intermediate-pressure
  • LP low-pressure
  • the power system 12 may include and/or exclude any of the plurality of thermal power systems 28, and thus the nuclear system 50, the combustion system 52, and the solar thermal system 54 may be used alone or in any combination with one another.
  • the combustion system 52 may include or exclude a gas turbine system having a compressor section, a combustor section, and a turbine section driven by hot combustion gases generated in the combustor section.
  • the steam turbine system 14 may receive one or more steam flows of the steam 62, 64, and/or 66 via steam circuits 68, 70, and 72, which include respective valves 74, 76, and 78.
  • the steam turbine system 14 may include any number or configuration of steam turbines, such as a high-pressure (HP) steam turbine 80, an intermediate-pressure (IP) steam turbine 82, and a low-pressure (LP) steam turbine 84.
  • HP high-pressure
  • IP intermediate-pressure
  • LP low-pressure
  • the steam turbine system 14 may direct the steam 62. 64. and/or 66 through any of the steam turbines 80, 82, and 84, depending on the conditions (e.g., pressure) of the steam 62. 64. and 66.
  • the steam turbine system 14 routes the steam 62. 64.
  • a steam circuit 86 routes intermediate-pressure steam to the IP steam turbine 82.
  • the intermediate-pressure steam flows through the IP steam turbine 82 to drive turbine blades, and then a steam circuit 88 routes low-pressure steam to the LP steam turbine 84.
  • the low-pressure steam flows through the LP steam turbine 84 to drive turbine blades, and then a condensate circuit 90 routes an output from the LP steam turbine 84 back to the steam generation system 16 (e.g., steam generator 56, 58, and/or 60).
  • the condensate circuit 90 includes a condenser 92 configured to condense any remaining steam into a condensate (e.g., condensed water), while the pump 94 is configured to pump the condensate back to the steam generation system 16.
  • the condensate circuit 90 also includes a valve 96 configured to control a flow of the condensate.
  • the steam turbines 80, 82, and 84 may be coupled to the same or different shafts 98 coupled to one or more loads 100, such as an electrical generator.
  • the electrical generator is configured to generate electricity for local usage or distribution on a power grid.
  • the power system 12 may be described as an electrical power generation system.
  • the nuclear system 50, the steam generator 56, the steam turbine system 14, and the load 100 may be defined as a nuclear- driven power generation system 102.
  • the combustion system 52, the steam generator 58, the steam turbine system 14, and the load 100 may be defined as a combustion-driven power generation system 104.
  • the solar thermal system 54, the steam generator 60, the steam turbine system 14, and the load 100 may be defined as a solar-driven power generation system 106.
  • the power system 12 may exclude the combustion system 52, while including one or more of the nuclear system 50 and/or the solar thermal system 54 to define a carbon-free power system.
  • the power system 12 serves as the heat source 26 (e.g., via one or more of the plurality of thermal power systems 28 and the steam generation system 16) to provide the thermal fluid 30 to the thermodynamic cycle 24 of the WHR system 22.
  • the thermodynamic cycle 24 is coupled to the power system 12 via one or more fluid circuits 110, which includes a supply circuit 112 and a return circuit 114.
  • the one or more fluid circuits 110 may include one or more valves, such as valves 1 16 and 118 coupled to the supply circuit 112 and the return circuit 114, respectively.
  • the valves 116 and 118 are configured to control the supply and return flows of the thermal fluid 30 between the power system 12 and the thermodynamic cycle 24.
  • the one or more fluid circuits 110 include a fluid circuit coupled to or passing through the nuclear system 50 and/or the steam generator 56, a fluid circuit coupled to or passing through the combustion system 52 and/or the steam generator 58, and fluid circuit coupled to or passing through the solar thermal system 54 and/or the steam generator 60.
  • the thermal fluid 30 may include heated water and/or steam from the steam generators 56, 58, and/or 60, the nuclear system 50, the combustion system 52, the solar thermal system 54, or any combination thereof.
  • the thermal fluid 30 may include or exclude hot combustion gases or flue gas from the combustion system 52.
  • the thermodynamic cycle 24 of the WHR system 22 is configured to transfer heat away from the thermal fluid 30 (e.g., hot or heated thermal fluid) received via the supply circuit 112 of the fluid circuit 110, transfer the heat into the working fluid 32 circulating in the thermodynamic cycle 24, produce electrical power or work with the thermodynamic cycle 24, and return the thermal fluid 30 (e.g., cool or cooled thermal fluid) back to the power system 12 via the return circuit 114 of the fluid circuit 110.
  • the thermodynamic cycle 24 may include a Brayton cycle, such as a closed-loop Brayton cycle.
  • the thermodynamic cycle 24 includes one or more compressors, one or more heat exchangers, and one or more turbines arranged in one or more fluid circuits.
  • the working fluid 32 may include one or more supercritical fluids (SCFs), inert gases such as noble gases, organic working fluids, or any combination thereof.
  • SCF may include a supercritical carbon dioxide (sCCh) or sCCh blend having one or more dopants.
  • the dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (CeFe), titanium tetrachloride (TiCB), or any combination of dopants.
  • the sCCh blend may have 5% to 20%mol dopants to increase the supercritical temperature of the sCCh.
  • the dopants may increase the critical temperature of the sCCh to about 70 to 100 degrees Celsius without a notable drop in efficiency.
  • the sCCh blend may increase the amount of waste heat quantity by condensing the sCCh blend at a higher temperature.
  • all or substantially all of the waste heat rejected from the thermodynamic cycle 24 is available for use with the DAC system 18 as the thermal fluid 34.
  • the thermodynamic cycle 24 may be described as a SCF-based cycle or a SCF cycle.
  • the noble gases may include helium (He), xenon (Xe), or a combination thereof (e.g., He-Xe mixture).
  • the inert gas may include nitrogen.
  • the organic working fluids may include hydrocarbons (HCs), fluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof.
  • the thermodynamic cycle 24 of the WHR system 22 is configured to use waste heat to support the DAC system 18.
  • the WHR system 22 includes one or more fluid circuits 130 extending between the thermodynamic cycle 24 and the DAC system 18 (e.g., gas capture systems 20).
  • the fluid circuits 130 may include one or more supply circuits 132 and one or more return circuits 134.
  • the fluid circuits 130 also include one or more valves, such as valves 136 and 138 disposed along the supply circuit 132 and the return circuit 134, respectively.
  • the valves 136 and 138 are configured to control the supply and return flows of the thermal fluid 34 between the thermodynamic cycle 24 and the gas capture systems 20 of the DAC system 18.
  • thermodynamic cycle 24 of the WHR system 22 is configured to transfer waste heat away from the working fluid 32 circulating in the thermodynamic cycle 24 and into the thermal fluid 34 (e.g., hot or heated thermal fluid) being supplied via the supply circuit 132.
  • the gas capture systems 20 of the DAC system 18 are configured to transfer heat away from the thermal fluid 34 (e.g.. hot or heated thermal fluid) received via the supply circuit 132, use the heat as needed to support the desorption mode or process, and then return the thermal fluid 34 (e.g., cool or cooled thermal fluid) back to the thermodynamic cycle 24 via the return circuit 134.
  • the thermal fluid 34 may contain heat (e.g., waste heat) in excess of the thermal needs in the gas capture systems 20 of the DAC system 18.
  • the WHR system 22 further includes a thermal storage system 140 have one or more thermal storage units or media 142, 144. 146, and 148.
  • Each of the thermal storage units or media 142, 144, 146, and 148 may include any suitable thermal energy storage (TES) technology', including sensible thermal energy storage, latent thermal energy storage, and/or thermochemical thermal energy storage.
  • the latent thermal energy storage may include phase change materials (PCMs).
  • the PCMs may include solid-liquid PCMs, solid-solid PCMs, solid-gas PCMs, liquid-gas PCMs, or any combination thereof.
  • the PCMs are configured to absorb heat during a phase transition and subsequently release heat when needed to support the DAC system 18.
  • the phase transition may be between solid and liquid phases for solid-liquid PCMs, or the phase transition may be between different solid states for solid-solid PCMs (e.g., different cry stalline structures).
  • the PCMs may include any suitable transition among or between solid, liquid, and gas phases.
  • the PCMs may be stored or housed in one or more enclosures, such as an interior chamber of a thermally insulated housing, a plurality of micro-encapsulations (e.g., micro capsules), or a combination thereof.
  • a solid-solid PCM may change cry stalline structure from one lattice configuration to another in an operating temperature range of 50 to 175 degrees Celsius.
  • a polyurethane PCM may have an operating temperature range of 20 to 36 degrees Celsius.
  • the operating temperature ranges may vary' for other solid-solid PCMs, such as polymer PCMs, and various solid-liquid PCMs, such as paraffins, inorganic salt hydrates ( teSO-i.lOFEO), bio- PCMs (e.g., organic fatty acid ester PCMs made from natural resources, such as soy beans and palm oils), and sodium acetate trihydrate (SAT, C2H9NaOs).
  • solid-solid PCMs such as polymer PCMs
  • various solid-liquid PCMs such as paraffins, inorganic salt hydrates ( teSO-i.lOFEO), bio- PCMs (e.g., organic fatty acid ester PCMs made from natural resources, such as soy beans and palm oils), and sodium acetate trihydrate (SAT, C2H9NaOs).
  • the WHR system 22 selectively enables heat transfer from the fluid circuit 130 to the thermal storage system 140 via a fluid circuit 150.
  • the fluid circuit 150 include a supply circuit 152 and a return circuit 154 extending between the thermal storage system 140 and the supply circuit 132 of the fluid circuit 130.
  • the fluid circuit 150 also includes one or more valves, such as valves 156 and 158 along the supply circuit 152 and the return circuit 154, respectively.
  • the valves 156 and 158 are configured to open, close, and generally adjust the supply and return flows of the thermal fluid 34 between the supply circuit 132 of the fluid circuit 130 and the thermal storage system 140.
  • thermal fluid 34 transfers heat to the thermal storage units or media 142, 144, 146, and 148 in the thermal storage system 140. If the thermal storage units or media 142, 144, 146, and 148 are completely thermally loaded and excess waste heat is still available, then the WHR system 22 may selectively direct the thermal fluid 34 to another system for use of the waste heat and/or the WHR system 22 may enable a waste heat discharge system 160 to discharge the waste heat into the atmosphere.
  • the waste heat discharge system 160 may include a heat exchanger 162 coupled to the thermal storage system 140 via a fluid circuit f64, wherein the fluid circuit 164 circulates the thermal fluid 34 and/or a coolant fluid through the heat exchanger 162 to discharge the waste heat into the atmosphere as indicated by arrow 166.
  • the thermal storage system 140 is configured to provide the stored heat to the gas capture systems 20 (e.g., as the thermal fluid 34).
  • the DAC system 18 includes one or more gas capture systems 20 configured to capture undesirable gases from air 190 and/or one or more other gases and output a treated gas (e.g., treated air 191) substantially free of the undesirable gases.
  • the gas capture systems 20 may include any one or any combination of gas capture systems 192 and 194, each having a plurality of components (e.g., components 196, 198, 200. and 202).
  • the gas capture systems 20 e.g., 192 and 194) are configured to obtain a captured gas 204 from the air 190.
  • the gas capture systems 20 may capture and output carbon dioxide (CO2) as the captured gas 204, which may further be directed to a compression system 206.
  • the compression system 206 may include one or more compressors configured to compress the captured gas 204 (e.g., CO2) and deliver the captured gas to storage and/or a pipeline 208.
  • the air 190 is compressed by one or more compressors 210 along an air intake circuit 212 coupled to the DAC system 18.
  • the captured gas 204 may be supplied to a system to create a new product, such as an input stream for liquefied carbon based fuel.
  • the gas capture systems 20 may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof, configured to remove and capture undesirable gases from the air 190 and/or other gases.
  • the gas capture systems 20 e.g., 192 and 194 may be configured to remove and capture undesirable gases, such as carbon oxides (COx) (e.g., carbon dioxide (CO2) and carbon monoxide (CO)), and thus the gas capture systems 20 may be described as carbon capture systems.
  • COx carbon oxides
  • CO2 carbon dioxide
  • CO2 carbon monoxide
  • the gas capture systems 20 may be configured to remove and capture undesirable gases, such as nitrogen oxides (NOx) (e.g., nitrogen dioxide (NO2)), and thus the gas capture systems 20 may be described as NOx capture systems.
  • NOx nitrogen oxides
  • the gas capture systems 20 e.g., 192 and 194 may be configured to remove and capture undesirable gases, such as sulfur oxides (SOx) (e.g., sulfur dioxide (SO2)). and thus the gas capture systems 20 may be described as SOx capture systems.
  • SOx sulfur oxides
  • the gas capture systems 20 e.g., 192 and 194 may be described as sorbent-based carbon capture systems using sorbent materials as an example and/or solvent based carbon capture systems using liquid absorbents (e.g., solvents) as an example.
  • the embodiments disclosed herein may use any type or configuration of gas capture systems 20 (e.g., 192 and 194) as noted above.
  • Each of the gas capture systems 20 may include components 196, 198, 200, and 202.
  • the components 196, 198, 200, and 202 may include sorbent materials disposed on or in ducts (e.g., adsorption duct, desorption duct, and cooling duct), contactors, cartridges, moving beds, rotating wheels, cartridges, or any combination thereof, along a flow path of the air 190.
  • the sorbent-based gas capture systems 20 are configured to adsorb the undesirable gases (e.g., CO2) into the sorbent materials in an adsorption mode and desorb the undesirable gases from the sorbent materials in a desorption mode.
  • the components 196, 198, 200. and 202 may include cooling systems to help control the temperature of the sorbent materials (e.g., maintain sorbent temperatures within upper and lower temperature thresholds) to improve efficiency of the adsorption mode.
  • the cooling systems may include heat exchangers (e.g., fin and tube heat exchangers), heat pipes, and other thermal control systems coupled to the sorbent materials to help control the temperature of the sorbent materials.
  • the components 196, 198, 200, and 202 also may include heating systems, such as heated fluid systems (e g., steam systems, electrical heaters, waste heat systems, etc.), configured to apply heat to the sorbent materials to desorb the undesirable gases from the sorbent matenals during the desorption mode.
  • heated fluid systems e g., steam systems, electrical heaters, waste heat systems, etc.
  • the thermodynamic cycle 24 and/or the thermal storage system 140 of the WHR system 22 is configured to provide the thermal fluid 34 to the sorbent materials during the desorption mode.
  • the components 196, 198, 200, and 202 also may include cooling systems, such as cooling fluid systems (e.g., gas cooling systems, liquid cooling systems, etc.), configured to apply a cooling fluid to the sorbent materials during a cooling mode.
  • the sorbent-based gas capture systems 20 also may include other suitable components 196, 198, 200, and 202 in support of the sorbent materials.
  • the components 196, 198, 200, and 202 may include one or more absorbers, one or more strippers, and a solvent circuit through the absorbers and strippers.
  • the absorber is configured to absorb the undesirable gases (e.g., CO2) into a solvent in an absorption mode, thereby outputting a treated gas (e.g., treated air or other gas) and a gas-rich solvent (e.g., CO2 rich solvent).
  • the stripper is configured to strip the undesirable gases from the gas-rich solvent in a desorption mode, thereby outputting a gas-lean solvent (e.g.. CO2 lean solvent) back to the absorber and outputting the captured gas 204.
  • a gas-lean solvent e.g.. CO2 lean solvent
  • the components 196, 198, 200, and 202 may include cooling systems coupled to the absorber, wherein the cooling systems are configured to extract heat generated by the absorption mode to help control the temperature of the solvent (e.g., maintain solvent temperatures within upper and lower temperature thresholds) to improve efficiency of the absorption mode.
  • the cooling systems may include heat exchangers (e.g.. fin and tube heat exchangers), heat pipes, and other thermal control systems coupled to the absorber to help control the temperature of the solvent.
  • the components 196, 198, 200, and 202 also may include heating systems, such as heated fluid systems (e.g., steam systems, electrical heaters, waste heat systems, etc.), coupled to the strippers, wherein the heating systems are configured to apply heat to the gas-rich solvent to desorb the undesirable gases from the gas-rich solvent during the desorption mode.
  • heated fluid systems e.g., steam systems, electrical heaters, waste heat systems, etc.
  • the thermodynamic cycle 24 and/or the thermal storage system 140 of the WHR system 22 is configured to provide the thermal fluid 34 to the gas-rich solvent during the desorption mode.
  • 198, 200, and 202 also may include a reboiler coupled to the stripper, pumps and valves to control a flow of the solvent through the solvent circuit between the absorber and the stripper, and heat exchangers to cool the gas-lean solvent supplied to the absorber and to heat the gas-rich solvent supplied to the stripper.
  • the solvent-based gas capture systems 20 also may include other suitable components 196. 198, 200, and 202 in support of the absorbers and strippers.
  • the combined cycle system 10 also includes a controller 220 coupled to the power system 12, the steam turbine system 14, the steam generation system 16, the DAC system 18, the WHR system 22 including the thermodynamic cycle 24 and the thermal storage system 140, and various sensors 222 distributed throughout the combined cycle system 10.
  • the controller 220 includes one or more processors 224. memory 226, instructions 228 stored on the memory 226 and executable by the processor 224, and communication circuitry 230 configured to communicate with the sensors 222 and various equipment throughout the combined cycle system 10.
  • the controller 220 is configured to control the nuclear system 50.
  • the controller 220 also may control the valves 74, 76, 78, and 96 and the pump 94 to facilitate control of the flows between the steam generators 56, 58, and 60 and the steam turbine systems 14.
  • the controller 220 is configured to control the valves 116 and 118 to control the flow of the thermal fluid 30 between the power system 12 and the thermodynamic cycle 24, thereby helping to control the heat transfer to the thermodynamic cycle 24.
  • the controller 220 is configured to control the valves 136 and 138 to control the flow of the thermal fluid 34 between the thermodynamic cycle 24 and the DAC system 18, thereby helping to control the heat transfer to the one or more gas capture systems 20 (e.g., 192 and 194).
  • the controller 220 is configured to control the valves 156 and 158 to control the flow of the thermal fluid 34 between the thermal storage system 140 and the fluid circuit 130, thereby helping to control the storage of excess heat and the release of stored heat for use in the one or more gas capture systems 20 (e.g., 192 and 194).
  • the controller 220 is configured to control operation of the gas capture systems 20 (e.g., 192 and 194), such by controlling modes of operation (e.g., adsorption mode, desorption mode, cooling mode), controlling the WHR system 22 (e.g.. the thermodynamic cycle 24 and the thermal storage system 140) to control the flow and temperature of the thermal fluid 34 provided to the gas capture systems 20, controlling flows of various fluids through the gas capture systems 20, or any combination thereof.
  • modes of operation e.g., adsorption mode, desorption mode, cooling mode
  • controlling the WHR system 22 e.g. the thermodynamic cycle 24 and the thermal storage system 140
  • the sensors 222 are configured to monitor various operational parameters of the combined cycle system 10.
  • the sensors 222 include temperature sensors, pressure sensors, flow rate sensors, fluid composition sensors (e.g., gas composition sensors), or any combination thereof.
  • the sensors 222 may monitor the parameters (e.g., temperature, pressure, flow rate, and fluid composition) at one or more locations of the DAC system 18, the WHR system 22, the thermodynamic cycle 24 (e.g., the working fluid 32), the thermal storage system 140, the thermal fluid 30, the thermal fluid 34, steam 62, 64, and/or 66, the steam generators 56, 58, and 60, the steam turbine systems 14, the nuclear system 50, the combustion system 52, the solar thermal system 54, or any combination thereof.
  • the parameters e.g., temperature, pressure, flow rate, and fluid composition
  • the sensors 222 may monitor the temperature of the thermal fluid 34 provided to the gas capture systems 20, the temperature of the sorbent materials in sorbent-based gas capture systems, the temperature of solvent in solvent-based gas capture systems, or any combination thereof.
  • the controller 220 may adjust the operating mode, fluid flows, heating, cooling, or any combination thereof, in the gas capture systems 20. Additionally, in response to the feedback from the sensors 222, the controller 220 may adjust the operating mode, fluid flows, heat transfer, compression in compressors, expansion in turbines, or any combination thereof, in the thermodynamic cycle 24.
  • the thermal fluid 34 may include a heated gas or liquid, such as a heated water and/or steam.
  • the thermal fluid 34 may be the same fluid or a different fluid from the working fluid 32 in the thermodynamic cycle 24. Additionally, in certain embodiments, the thermal fluid 34 may be the same fluid or a different fluid from the fluid used in the gas capture systems 20.
  • a heat exchanger may transfer heat from the working fluid 32 (e.g., waste heat rejection) to the thermal fluid 34 at a temperature suitable to enable desorption of the undesirable gas (e.g., CO2) in the one or more gas capture systems 20.
  • the temperature of the working fluid 32 at the one or more locations in the thermodynamic cycle 24 may be 1 0 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, or 130 to 150 degrees Celsius.
  • the waste heat rejection from the working fluid 32 to the thermal fluid 34 may occur at a temperature of at least equal to or greater than 100, 110, 120, 130, 140, or 150 degrees Celsius.
  • the thermal fluid 34 may provide heat in the one or more gas capture systems 20 to enable desorption in a similar temperature range of 100 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, 130 to 150 degrees Celsius, or 110 to 130 degrees Celsius.
  • the thermal fluid 34 may be provided to the gas capture systems 20 to support desorption at a temperature of at least equal to or greater than 100, 110, 120, 130, 140, or 150 degrees Celsius, plus or minus 5 degrees Celsius.
  • FIG. 2 is a schematic of an embodiment of a gas capture system 20 of the DAC system 18 of FIG. 1, illustrating a sorbent-based gas capture system 250.
  • the sorbent-based gas capture system 250 includes a plurality of sorbent-based gas capture assemblies or units 252 (e.g., adsorbers or adsorption units) associated with a plurality of respective conduits 254, such as conduits 256, 258, and 260 (e.g., sorbent-containing conduits).
  • the sorbent-based gas capture units 252 may include temperature swing adsorption (TSA) units or adsorbers, wherein a temperature swing or change is used to alternatively operate in an adsorption mode at a first temperature and a desorption mode at a second temperature. The first temperature is lower than the second temperature.
  • TSA temperature swing adsorption
  • the lower first temperature enables the sorbent-based gas capture units 252 to adsorb the undesirable gas, where lower temperatures generally increase a capacity for adsorbing the undesirable gas.
  • the higher second temperature enables the sorbent-based gas capture units 252 to desorb the undesirable gas, which can then be captured and used in other downstream processes.
  • the sorbent-based gas capture units 252 include sorbent-based gas capture units 252A, 252B, and 252C associated with the conduits 256, 258, and 260.
  • the conduits 254 e.g., 256. 258, and 260
  • the conduits 254 may be sorbent-lined along interior surfaces, sorbent-packed within interior volumes, or generally filled with at least 10, 20, 30, 40, 50, 60, 70, 80, 90, or more percent by volume of sorbent material.
  • the sorbent-based gas capture unit 252 may include any number of conduits 254, such as 2, 3, 4, 5, 6, 7, 8. 9, 10, or more, which are configured in parallel and/or series.
  • Each of the conduits 254 e.g., 256.
  • each of the conduits 254 (e.g., 256, 258, and 260) may include a contactor assembly 278 having any number of the contactors 280, such as 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more contactors 280.
  • Each of the contactors 280 has a body 284 with the exterior surface 276 disposed about an interior portion 286.
  • the sorbent material 272 is disposed along the exterior surface 276, while the interior portion 286 includes a material 282 different than the sorbent material 272.
  • the body 284 may be a solid body throughout the interior portion 286, wherein the body 284 is at least substantially or completely made with the sorbent material 272 throughout the interior portion 286 to the exterior surface 276.
  • the body 284 may be a hollow body in the interior portion 286 (e.g., interior chamber or cavity), wherein the body 284 has an outer wall 288 disposed about the interior portion 286.
  • the interior portion 286 may include a heat exchange circuit or flow path extending throughout the body 284 between a fluid inlet and a fluid outlet, which may be coupled to a heat exchange circuit for cooling and/or heating.
  • the interior portion 286 may be configured to circulate a cooling fluid during an adsorption mode, a heating fluid (e.g., the thermal fluid 34 from the thermodynamic cycle 24) during a desorption mode, and a cooling fluid during a cooling mode of the sorbent-based gas capture system 250.
  • the gas capture system 20 is configured to sequentially and repeatedly operate in a cycle of: (1) an adsorption mode, (2) a desorption mode, and (3) a cooling mode for each of the sorbent-based gas capture units 252A, 252B. and 252C.
  • the temperature of the sorbent material 272 directly affects the adsorption efficiency of the sorbent material 272 during the adsorption mode.
  • the sorbent material 272 may have an optimal temperature or temperature range for efficient adsorption of the undesirable gases.
  • the adsorption of the undesirable gases into the sorbent material 272 is an exothermic process, which generates heat that generally increases the temperature of the sorbent material 272 and reduces its adsorption efficiency without any cooling of the sorbent material 272.
  • the disclosed embodiments may control the cooling of the sorbent material 272 during the adsorption mode to improve the adsorption efficiency.
  • the temperature of the sorbent material 272 directly affects the desorption efficiency of the sorbent material 272 during the desorption mode.
  • the sorbent material 272 may- have an optimal temperature or temperature range for efficient desorption of the undesirable gases.
  • the disclosed embodiments may control the heating of the sorbent material 272 during the desorption mode to improve the desorption efficiency.
  • the controller 220 may be configured to control the WHR system 22 (e.g.. the thermodynamic cycle 24 and the thermal storage system 140) to control the thermal fluid 34 supplied to each of the sorbent-based gas capture units 252A, 252B, and 252C during the desorption mode alone or in combination with other heated fluids.
  • WHR system 22 e.g. the thermodynamic cycle 24 and the thermal storage system 140
  • the adsorption mode may be configured to adsorb undesirable gas from a gas 340 into the sorbent material 272 at a first temperature
  • the desorption mode may be configured to desorb the undesirable gas from the sorbent material 272 using a heat source (e.g., thermal fluid 34) at a second temperature
  • the cooling mode may 7 be configured to cool the sorbent material 272 using a cooling source (e.g., cooling fluid) at a third temperature, wherein the second temperature is greater than the first and third temperatures, and the third temperature is lesser than the first and third temperatures.
  • the first temperature may be approximately 40 degrees Celsius (e g., plus or minus 5, 10, 15, or 20 degrees Celsius)
  • the second temperature may be equal to or greater than approximately 100, 110, 120, 130, 140, or 150 degrees Celsius
  • the third temperature may be less than or equal to approximately 0, 5. 10, 15, 20, 25, or 30 degrees Celsius.
  • the gas capture system 20 includes a thermal control system 290 having a fluid circulation system 292.
  • one or more fluid circulation circuits 294 e.g., fluid conduits, manifolds, valves, etc.
  • the heat exchangers 296 may include one or more heat exchange flow paths coupled to and/or extending through each contactor assembly 278.
  • the heat exchangers 296 also may include a plurality of heat pipes 298, wherein each contactor assembly 278 includes one or more heat pipes 298 coupled to and/or extending through each contactor 280 in the contactor assembly 278.
  • the fluid circulation system 292 may include a plurality of components, such as components 300, 302, and 304, such as heat exchangers, pumps, valves, coolant supplies, or any combination thereof.
  • the thermal control system 290 may circulate a thermal fluid (e.g., liquid or gas thermal fluid) from the fluid circulation system 292 through the fluid circulation circuits 294 and the heat exchangers 296 to exchange heat between the thermal fluid and the contactors 280 and the sorbent materials 272 during any one or all of the operating modes (e.g., adsorption mode, desorption mode, and/or cooling mode).
  • a thermal fluid e.g., liquid or gas thermal fluid
  • the fluid circulation circuits 294 may include independent fluid circulation circuits for each of the contactor assemblies 278, such that the thermal control system 290 can independently control the temperature for each of the contactor assemblies 278 depending on the operating modes (e.g., adsorption mode, desorption mode, and/or cooling mode) of the sorbent-based gas capture units 252A, 252B, and 252C.
  • the thermal control system 290 is configured to circulate the thermal fluid (e.g., coolant or cooling fluid at a relatively lower temperature) during the adsorption mode and the cooling mode, thereby cooling the contactors 280 and the sorbent materials 272.
  • the thermal control system 290 is configured to circulate the thermal fluid (e.g., heated or heating fluid at a relatively higher temperature) during the desorption mode, thereby heating the contactors 280 and the sorbent materials 272 to facilitate desorption.
  • the thermal fluid may include the thermal fluid 34 from the WHR system 22 (e.g., the thermodynamic cycle 24 and the thermal storage system 140) during the desorption mode.
  • the sorbent material 272 may cover, coat, or generally line at least 50, 60, 70, 80, 90, 95, or 100 percent of the interior surface 274 of the outer conduit wall 262. the exterior surface 276 of the contactors 280. and/or other structures within the conduits 254.
  • the contactors 280 may include rectangular plates, airfoil shaped panels, a parallel arrangement of tubes, a grid arrangement of tubes, a plurality of cartridges, radial projections, baffles, fins, honeycomb structures, a plurality of contactor elements supported in a bundle, or any combination thereof.
  • the plurality of contactor elements may include a plurality' of particles, beads, strips, strands, mesh, or other distributed structures, which leave voids for fluid flow. Additionally or alternatively, the sorbent material 272 may at least partially fill or pack an interior volume of the central bore or interior surface 274, such that voids remain to facilitate fluid flow (e.g., a void fraction of less than or equal to 10, 20, 30, 40, or 50 percent).
  • the central axis 266 extending from the inlet 268 to the outlet 270 may define the flow path 264 as a linear flow path, a curved flow path, a winding or serpentine flow path, a spiral or helical flow path, a tortuous flow path, an expanding and contracting flow path, a flow path with splits and/or unions, or any combination thereof.
  • the flow path 264 may be defined as a tortuous flow path and include any number or configuration of the foregoing flow paths.
  • the sorbent material 272 may include one or more sorbent materials configured to adsorb the undesirable gases, such as sorbent materials designed or suitable for adsorption of carbon oxides (COx) such as carbon dioxide (CO2) and carbon monoxide (CO), nitrogen oxides (NOx), sulfur oxides (SOx) such as sulfur dioxide (SO2), methane (CFU), or any other undesirable gases as described herein or subject to regulations and/or considered greenhouse gases.
  • the sorbent materials 272 may include porous, solid-phase materials, including mesoporous silicas, zeolites (e.g., aluminosilicates), and metal-organic frameworks (MOFs) and covalent organic frameworks (COFs).
  • the foregoing sorbent materials 272 may be particularly well-suited for CO2 adsorption in the sorbent-based gas capture unit 252. However, any suitable sorbent materials 272 may be used depending on the desired target for gas capture of undesirable gases. In certain embodiments, a plurality of the sorbent-based gas capture systems 250 may be used in series, wherein each of the sorbent-based gas capture system 250 uses the same or different sorbent materials 272 to remove and capture the same or different undesirable gases in stages.
  • the sorbent-based gas capture system 250 may be configured to alternate each of the sorbent-based gas capture units 252A, 252B, and 252C associated with the conduits 256, 258, and 260 between the adsorption mode (e.g., adsorbing the undesirable gases into the sorbent material 272), the desorption mode (e.g., desorbing the undesirable gases from the sorbent material 272), and the cooling mode (e.g., cooling the sorbent material 272) using the controller 220 and the sensors 222.
  • the adsorption mode e.g., adsorbing the undesirable gases into the sorbent material 272
  • the desorption mode e.g., desorbing the undesirable gases from the sorbent material 272
  • the cooling mode e.g., cooling the sorbent material 272
  • the controller 220 is configured to control the sorbent-based gas capture system 250 to perform a staggered operational cycle of the sorbent-based gas capture units 252A, 252B, and 252C between the different operating modes (e.g., adsorption mode, desorption mode, and cooling mode). For example, for a first duration of time, the controller 220 may operate the sorbent-based gas capture unit 252A in the adsorption mode, the sorbent-based gas capture unit 252B in the desorption mode, and the sorbent-based gas capture unit 252C in the cooling mode.
  • the controller 220 may operate the sorbent-based gas capture unit 252A in the adsorption mode, the sorbent-based gas capture unit 252B in the desorption mode, and the sorbent-based gas capture unit 252C in the cooling mode.
  • the controller 220 may operate the sorbent-based gas capture unit 252A in the desorption mode, the sorbent-based gas capture unit 252B in the cooling mode, and the sorbent-based gas capture unit 252C in the adsorption mode.
  • the controller 220 may operate the sorbent-based gas capture unit 252A in the cooling mode, the sorbent-based gas capture unit 252B in the adsorption mode, and the sorbent-based gas capture unit 252C in the desorption mode.
  • the sorbent-based gas capture system 250 also may be configured to simultaneously operate multiple units (e.g., 2, 3, 4, or more) of the sorbent-based gas capture units 252 in each of the operating modes, such as multiple units 252 in the adsorption mode, multiple units 252 in the desorption mode, and multiple units 252 in the cooling mode.
  • the multiple units 252 may be arranged in series, in parallel, or a combination thereof.
  • the controller 220 is configured to alternate the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) between the adsorption, desorption, and the cooling modes via a plurality of support systems.
  • the support systems may include the thermal control system 290, an upstream flow distribution system 310, and a downstream flow' distribution system 312.
  • the upstream flow distribution system 310 includes a gas supply system 314 (or gas intake system), a heating fluid supply system 316 (e.g., heated gas and/or heated liquid supply system), and a cooling fluid supply system 318, while the downstream flow' distribution system 312 includes a post-adsorption processing system 320 (e.g., after the adsorption mode), a post-desorption processing system 322 (e.g., fluid processing system after the desorption mode), and a post-cooling system 324 (e.g., after the cooling mode).
  • the gas supply system 314 of the upstream flow distribution system 310 is configured to provide a gas 340 (e.g., air 190 and/or other gas) to enable the adsorption mode when selectively operating each of the sorbent-based gas capture units 252 (e.g.. 252A, 252B. and 252C) in the adsorption mode via the controller 220.
  • a gas 340 e.g., air 190 and/or other gas
  • the gas 340 may include exhaust gas, flue gas, or other combustion gases alone or in combination with the air 190.
  • the gas supply system 314 includes a gas pretreatment system 330 having one or more gas pre-treatment components 332.
  • the gas pretreatment component 332 may include a thermal control component (e.g., gas temperature control component), such as a heat exchanger, a heater, a cooler, or any combination thereof, configured to adjust (e.g., increase or decrease) a temperature of the gas 340.
  • the heat exchanger may exchange heat with water, exhaust gas, compressor bleed flow, waste heat, one or more of the heat sources 26, or some other thermal fluid.
  • a waste heat recovery system may be used for heat transfer in the heat exchanger.
  • the gas pre-treatment component 334 may include a pressure control component, such as a pressure regulator, an expander or expansion chamber, a constrictor or constriction chamber, a fan or pump to add energy, a turbine to extract energy, or another suitable pressure controller.
  • the gas pre-treatment component 336 may include one or more contaminant removal units, such as a particulate filter, a moisture removal unit or dr er, a chemical removal unit, and/or other removal units configured clean the gas 340.
  • the gas pretreatment component 336 may include a humidity controller configured to maintain a desired relative humidity of the gas 340 being received into the sorbent-based gas capture system 250.
  • the gas supply system 314 also may include one or more valves 342 configured to control the distribution of the gas 340 to the plurality of conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 344, 346. and 348.
  • valves 342 configured to control the distribution of the gas 340 to the plurality of conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 344, 346. and 348.
  • valves 342 may include one or more multi-way valves and/or distribution manifolds to independently distribute the gas 340 through the distribution conduits 344, 346, and/or 348 to the respective sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) when operating in an adsorption mode in response to control signals from the controller 220.
  • the respective sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • the heating fluid supply system 316 of the upstream flow distribution system 310 is configured to supply a heating fluid to enable the desorption mode when selectively operating each of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) in the desorption mode via the controller 220.
  • the heating fluid supply system 316 also may coordinate with a vacuum system of the post-desorption processor 442.
  • the heating fluid supply system 316 includes one or more heating fluid supplies 350, such as one or more steam supplies, heated water supplies, heated gas supplies, and/or waste heat supplies.
  • the heating fluids also may be described as sweep fluids, such as a sweep gas or a sweep steam.
  • the heating fluid supplies 350 may include the steam turbine system 14.
  • the heating fluid supplies 350 may be configured to supply a heating fluid 352 (e.g., steam and/or heated water) and/or a heating fluid 354 (e.g., waste heat recovery fluid, such as thermal fluid 34) to a heating fluid control 356 of the heating fluid supply system 316.
  • a heating fluid 352 e.g., steam and/or heated water
  • a heating fluid 354 e.g., waste heat recovery fluid, such as thermal fluid 34
  • the heating fluid 352 and/or 354 may include a heated liquid and/or a heated gas, such as heated CO2, air, inert gas such as nitrogen, noble gas, water, oil, or any combination thereof.
  • the thermodynamic cycle 24 uses waste heat recovered from the thermal power systems 28 (e.g., nuclear system 50. combustion system 52, and/or solar thermal system 54) via the WHR system 22, and provides the thermal fluid 34 for use as the heating fluid 354.
  • the thermal fluid 34 (e.g., waste heat recovery' fluid) also may be described as an excess heat or waste heat recovered for use in the heating fluid supply system 316 of the sorbent-based gas capture units 252.
  • the thermal storage system 140 stores waste heat and/or provides waste heat as the thermal fluid 34 for use as the heating fluid 354.
  • the heating fluid control 356 includes one or more heating fluid control components 358, 360. and 362. which may be configured to process, adjust, and/or control characteristics of the heating fluid 352 and/or heating fluid 354 upstream from the conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C).
  • the heating fluid control component 358 may include a thermal control component (e.g., temperature control component), such as a heat exchanger, a heater, a cooler, or any combination thereof, configured to adjust (e.g., increase or decrease) a temperature of the heating fluid 352 and/or the heating fluid 354.
  • the heat exchanger may exchange heat with water, lubricant, coolant, refrigerant, or some other thermal fluid.
  • a waste heat recovery system may be used for heat transfer in the heat exchanger.
  • the heating fluid control component 360 may include a pressure control component, such as a pressure regulator, an expander or expansion chamber, a constrictor or constriction chamber, a fan or pump to add energy, a turbine to extract energy, or another suitable pressure controller.
  • the heating fluid control component 362 may include a pretreatment component, such as a particulate filter, a cold water drain, and/or other pretreatment components configured to alter characteristics of the heating fluid 352 and/or the heating fluid 354 or remove contaminants.
  • the heating fluid supply system 316 also may include one or more valves 364 configured to control the distribution of the heating fluid 352 (e.g., steam and/or heated water) and/or the heating fluid 354 (e.g., waste heat recovery fluid) to the plurality of conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 366, 368, and 370.
  • the heating fluid 352 e.g., steam and/or heated water
  • the heating fluid 354 e.g., waste heat recovery fluid
  • valves 364 may include one or more multi-way valves and/or distribution manifolds to independently distribute the heating fluid 352 and/or the heating fluid 354 through the distribution conduits 366, 368, and 370 to the respective sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) when operating in a desorption mode in response to control signals from the controller 220.
  • the respective sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • the cooling fluid supply system 318 of the upstream flow distribution system 310 is configured to supply a cooling fluid to enable the cooling mode when selectively operating each of the sorbent-based gas capture units 252 (e.g.. 252A, 252B, and 252C) in the cooling mode via the controller 220.
  • the cooling fluid supply system 318 includes one or more cooling fluid supplies 372, such as one or more water supplies, cooled air supplies, cooled inert gas (e.g., nitrogen) supplies, cooled CO2 supplies, or any combination thereof.
  • the cooling fluid supplies 372 may be configured to supply a coolant or cooling fluid 374 (e.g., liquid or gas coolant) to a cooling fluid control 376 of the cooling fluid supply system 318.
  • the cooling fluid control 376 includes one or more cooling fluid control components 378, 380, and 382. which may be configured to process, adjust, and/or control characteristics of the cooling fluid 374 upstream from the conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C).
  • the cooling fluid control component 378 may include a thermal control component (e.g., temperature control component), such as a heat exchanger, a heater, a cooler, or any combination thereof, configured to adjust (e.g., increase or decrease) a temperature of the cooling fluid 374.
  • the heat exchanger may exchange heat with water, lubricant, coolant, refrigerant, or some other thermal fluid.
  • the cooling fluid control component 380 may include a pressure control component, such as a pressure regulator, an expander or expansion chamber, a constrictor or constriction chamber, a fan or pump to add energy, a turbine to extract energy, or another suitable pressure controller.
  • the cooling fluid control component 382 may include a pre-treatment component, such as a particulate filter and/or other pretreatment components, configured to alter characteristics of the cooling fluid 374 or remove contaminants.
  • the cooling fluid supply system 318 also may include one or more valves 384 configured to control the distribution of the cooling fluid 374 (e.g., liquid or gas coolant) to the plurality of conduits 254 (e.g.. 256, 258. and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 386, 388, and 390.
  • the cooling fluid 374 e.g., liquid or gas coolant
  • the plurality of conduits 254 e.g. 256, 258. and 260
  • the sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • valves 384 may include one or more multi-way valves and/or distribution manifolds to independently distribute the cooling fluid 374 through the distribution conduits 386, 388, and 390 to the respective sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) when operating in a cooling mode in response to control signals from the controller 220.
  • the respective sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • the controller 220 is configured to control the upstream flow distribution system 310 to altematingly distribute flows of the gas 340 during the adsorption mode, the heating fluid 352 and/or the heating fluid 354 in the desorption mode, and the cooling fluid 374 in the cooling mode to the different sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) having sorbent material 272.
  • the different sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C having sorbent material 272.
  • the gas 340 (e.g., air 190 and/or other gases) flows through the conduit 254 of the selected sorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) and contacts the sorbent material 272 disposed on the interior surface 274 of the outer conduit wall 262 and/or the exterior surface 276 of the contactors 280, such that the sorbent material 272 adsorbs the undesirable gases (e.g., CO2) from the gas 340.
  • the thermal control system 290 may circulate a coolant through the heat exchanger 296 to provide cooling of the contactors 280 and the sorbent material 272 during the adsorption mode.
  • the thermal control system 290 also may facilitate heat transfer to the coolant via a plurality of heat pipes 298 of the heat exchanger 296.
  • the sorbent-based gas capture unit 252 then discharges a treated gas 400 (e.g.. lean or substantially free of the undesirable gases) to the post-adsorption processing system 320.
  • the heating fluid 352 and/or the heating fluid 354 flows through the conduit 254 of the selected sorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) and contacts the sorbent material 272 disposed on the interior surface 274 of the outer conduit wall 262 and/or the exterior surface 276 of the contactors 280, thereby heating the sorbent material 272 to facilitate desorption of the undesirable gases (e.g., CO2) from the sorbent material 272.
  • the desorption mode may be configured to indirectly heat the sorbent material 272 via a heating circuit (e.g., heating conduit) extending through the sorbent-based gas capture unit 252.
  • the thermal control system 290 may circulate a heating fluid (e.g., heating fluid 352 and/or heating fluid 354) through the heat exchanger 296 to provide heating of the contactors 280 and the sorbent material 272.
  • a heating fluid e.g., heating fluid 352 and/or heating fluid 354
  • the heating fluid 354 may include the thermal fluid 34 from the thermodynamic cycle 24.
  • the thermal control system 290 also may facilitate heat transfer from the heating fluid across the contactors 280 via the plurality of heat pipes 298 of the heat exchanger 296.
  • the sorbent-based gas capture unit 252 then discharges a fluid flow 402 including the undesirable gas, the heating fluid 352, and/or the heating fluid 354 for further processing by the post-desorption processing system 322.
  • the cooling fluid 374 flows through the conduit 254 of the selected sorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) and contacts the sorbent material 272 disposed on the interior surface 274 of the outer conduit wall 262 and/or the exterior surface 276 of the contactors 280, thereby cooling the sorbent material 272 and the contactors 280.
  • the cooling mode may be configured to indirectly cool the sorbent material 272 and the contactors 280 via a cooling circuit (e.g., cooling conduit) extending through the sorbent-based gas capture unit 252.
  • the thermal control system 290 may circulate a cooling fluid through the heat exchanger 296 to provide cooling of the contactors 280 and the sorbent material 272.
  • the thermal control system 290 also may facilitate heat transfer away from the contactors 280 and the sorbent material 272 via the plurality of heat pipes 298 of the heat exchanger 296.
  • the cooling mode is configured to cool and regenerate the sorbent material 272 prior to a subsequent adsorption mode.
  • the sorbent-based gas capture unit 252 then discharges a fluid flow 404 (e.g., cooling fluid 374) for handling by the post-cooling system 324.
  • the sorbent-based gas capture system 250 includes a movable sorbent system configured to continuously or periodically move the sorbent material 272 between the adsorption mode, the desorption mode, and the cooling mode.
  • the sorbent-based gas capture system 250 may include a rotating contactor assembly or wheel (e.g., rotating contactors with sorbent material 272) configured to rotate from adsorption, desorption and cooling, thereby providing a continuous stream of captured undesirable gases.
  • the wheel e.g., rotating contactors with sorbent material 272
  • the wheel may extend into each of the plurality of conduits 254, and continuously rotate through the conduits 254.
  • one or more of the conduits 254 flow the gas 340 being treated to remove the undesirable gases, while one or more of the conduits 254 simultaneously flow the heating fluid 352 and/or heating fluid 354 to remove and capture the undesirable gas (e.g., CO2) to generate the captured gas 204. and while one or more of the conduits 254 simultaneously flow the cooling fluid 374 to regenerate the sorbent material 272.
  • the heating fluid 352 and/or heating fluid 354 may be routed or generally configured to provide direct heat transfer and/or indirect heat transfer to the sorbent material 272. thereby helping to separate and capture the undesirable gas.
  • the controller 220 is configured to control the downstream flow distribution system 312 to altematingly distribute flows from each sorbent-based gas capture unit 252 (e.g., 252A, 252B. and 252C) to route the treated gas 400 to the post-adsorption processing system 320 during the adsorption mode, the fluid flow' 402 (e.g., the undesirable gas, the heating fluid 352, and/or the heating fluid 354) to the post-desorption processing system 322 in the desorption mode, and the fluid flow' 404 (e.g., cooling fluid 374) to the post-cooling system 324 in the cooling mode.
  • each sorbent-based gas capture unit 252 e.g., 252A, 252B. and 252C
  • the fluid flow' 402 e.g., the undesirable gas, the heating fluid 352, and/or the heating fluid 354
  • the fluid flow' 404 e.g., cooling fluid 374
  • the downstream flow distribution system 312 includes one or more valves 410 fluidly coupled with the sorbent-based gas capture unit 252A, one or more valves 412 fluidly coupled with the sorbent-based gas capture unit 252B, and one or more valves 414 fluidly coupled with the sorbentbased gas capture unit 252C.
  • the valves 410 may include one or more multi-way valves and/or distribution manifolds coupled to distribution conduits 416, 418, and 420, which are coupled to the post-adsorption processing system 320, the postdesorption processing system 322, and the post-cooling system 324, respectively.
  • the valves 412 may include one or more multi-way valves and/or distribution manifolds coupled to distribution conduits 422.
  • valves 414 may include one or more multi-way valves and/or distribution manifolds coupled to distribution conduits 428, 430, and 432, which are coupled to the post-adsorption processing system 320, the post-desorption processing system 322, and the post-cooling system 324, respectively.
  • the controller 220 is configured to control the valves 410, 412, and 414 to independently control the flows from the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) to the post-adsorption processing system 320 in the adsorption mode, to the post-desorption processing system 322 in the desorption mode, and to the post-cooling system 324 in the cooling mode.
  • the sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • the post-adsorption processing system 320 includes a treated gas processing system 440, which may include a gas discharge outlet or stack, an additional gas treatment system, or any other suitable post processing equipment. In certain embodiments, the post-adsorption processing system 320 may combine multiple discharge gases into a single outlet or stack. In certain embodiments, when the gas 340 is the air 190, the treated gas may be used for ventilation and/or other uses benefiting from treated air.
  • the post-desorption processing system 322 may include a post-desorption processor 442 having one or more post-desorption processing components 444. 446, and 448.
  • the fluid flow 402 directed to the post-desorption processor 442 is a result of the desorption mode, wherein the heating fluid 352 (e.g.. steam and/or heated water) and/or heating fluid 354 (e.g., waste heat recover fluid, such as thermal fluid 34) is directed through the conduit 254 of the sorbent-based gas capture unit 252 (e.g., 252 A, 252B, or 252C) to desorb the undesirable gases (e.g., CO2) from the sorbent material 272.
  • the heating fluid 352 e.g. steam and/or heated water
  • heating fluid 354 e.g., waste heat recover fluid, such as thermal fluid 34
  • the one or more post-desorption processing components 444, 446, and 448 may be configured to process, adjust, and/or control characteristics of the fluid flow 402 (e.g., steam, heated water, and/or other fluid flow) from the conduits 254 (e.g., 256, 258, and 260) of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C).
  • the fluid flow 402 e.g., steam, heated water, and/or other fluid flow
  • the conduits 254 e.g., 256, 258, and 260
  • the sorbent-based gas capture units 252 e.g., 252A, 252B, and 252C
  • the post-desorption processing component 444 may include a captured gas/heated fluid separator configured to separate the heating fluid 352 (e.g., steam and/or heated water) and/or the heating fluid 354 from the captured gas, thereby outputting a fluid 450 (e.g., water condensate or other separated fluid) and the captured gas 204.
  • a captured gas/heated fluid separator include thermal control components, pressure control components, chemical separation components, or a combination thereof.
  • the captured gas/heated fluid separator may be configured to condense or cool the heating fluid 352 (e g., steam) using a condenser.
  • the post-desorption processing component 446 may include one or more removal units configured to remove contaminants from the fluid 450 and/or the captured gas 204.
  • the removal units may include particulate filters and/or water treatment units.
  • the removal units may include particulate filters, water removal units or dry ers, or further gas treatment units.
  • the post-desorption processing component 448 may include one or more pressure control components and/or flow control components, such as one or more pumps for the fluid 450 and one or more compressors for the captured gas 204.
  • the post-desorption processing components 448 also may include a vacuum system having one or more vacuum pumps configured to suction the captured gas/heated fluid flow from the sorbentbased gas capture units 252. In other words, the vacuum pumps are configured to create a low-pressure environment to help draw the captured gas/heated fluid flow from the sorbent-based gas capture units 252.
  • the post-cooling system 324 may include a cooling fluid recirculation system 452, which is configured to recirculate the fluid flow 404 back to the cooling fluid supply system 318 as the cooling fluid 374.
  • the cooling fluid recirculation system 452 may include components 454, 456, and 458, such as a recirculation pump, compressor, or booster fan, a cooling system, and flow' control valves.
  • the cooling system may include a heat exchanger configured to transfer heat away from the fluid flow 404, thereby cooling the fluid flow for additional use as the cooling fluid 374.
  • the heat available from the fluid flow 404 may be recovered in one or more heat exchangers to heat the heating fluid 352 and/or heating fluid 354 of the heating fluid supply system 316, thereby reducing the total heating energy demand. The remaining low grade heat from the fluid flow 404 may then be rejected to ambient.
  • the controller 220 is configured to receive feedback from the sensors 222 to facilitate adjustments of various operating parameters and change operating modes (e.g., adsorption mode, desorption mode, and cooling mode) of the sorbent-based gas capture units 252 (e.g.. 252A, 252B. and 252C).
  • various operating parameters and change operating modes e.g., adsorption mode, desorption mode, and cooling mode
  • the controller 220 may be configured to alternate flows (e.g...
  • the conduit 254 receives a flow of the gas 340, adsorbs the undesirable gases (e.g., CO2) from the gas 340 into the sorbent material 272, and outputs a treated gas 400 with a reduced content or concentration level of the undesirable gases.
  • undesirable gases e.g., CO2
  • the adsorption of undesirable gases into the sorbent material 272 is an exothermic process, which generates heat.
  • the thermal control system 290 including the heat exchangers 296 and the heat pipes 298, help to regulate the temperature of the sorbent material 272 during the adsorption mode, thereby maintaining or increasing the adsorption efficiency of the sorbent material 272.
  • the conduit 254 receives a flow of the heating fluid 352 (e.g., steam and/or heated water) and/or heating fluid 354, desorbs the undesirable gases (e.g..
  • the conduit 254 receives a flow of the cooling fluid 374 (e.g., gas or liquid coolant), thereby cooling the sorbent material 272 and the contactors 280.
  • the cooling fluid 374 e.g., gas or liquid coolant
  • the controller 220 is configured to monitor the sensors 222, such as sensors 222 at or upstream from the inlets 266 and sensors 222 at or downstream from the outlets 268, to evaluate rates of adsorption, desorption, and cooling, concentration levels of the undesirable gases, and other characteristics impacting the operating modes of the sorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C). If the sensors 222 indicate a need to alternate operating modes (e.g., adsorption, desorption, and cooling modes) of the sorbent-based gas capture units 252 (e.g., 252A, 252B. and 252C), then the controller 220 may be configured to control the valves 342. 364, 384, 410.
  • the sensors 222 such as sensors 222 at or upstream from the inlets 266 and sensors 222 at or downstream from the outlets 268, to evaluate rates of adsorption, desorption, and cooling, concentration levels of the undesirable gases, and other characteristics impacting the operating modes of the sorbent
  • the sensors 222 also may monitor the temperature of the sorbent material 272 and adjust the thermal control system 290 to provide heating or cooling depending on the operating mode (e.g., cooling during the adsorption and cooling modes and heating during the desorption mode).
  • the controller 220 may be configured to control the gas pre-treatment system 330 to control characteristics of the gas 340 (e.g., temperature, pressure, flow rate, etc.). Similarly, the controller 220 is configured to control the treated gas processing system 440 to control the processing of the treated gas 400 discharged from one or more of the conduits 254.
  • the heating fluid 352 e.g., steam and/or heated water
  • the heating fluid 354 e.g...
  • the controller 220 may be configured to control the steam generation system 16, the steam turbine system 14, the WHR system 22 (e.g., the thermodynamic cycle 24 and the thermal storage system 140), the heating fluid control 356, or any combination thereof, to control characteristics of the heating fluid 352 and/or the heating fluid 354 (e.g.. temperature, pressure, flow rate, steam content, water content, etc ).
  • the controller 220 is configured to control the post-desorption processor 442 to control the processing of the fluid flow 402 (including the undesirable gas desorbed during the desorption mode) discharged from one or more of the conduits 254.
  • the controller 220 may be configured to control the cooling fluid control 376 and/or the cooling fluid recirculation system 452 to control characteristics of the cooling fluid 374 (e.g., temperature, pressure, flow rate, etc.). Similarly, the controller 220 is configured to control the cooling fluid recirculation system 452 to control the processing of the fluid flow 404 (e.g., cooling fluid 374) discharged from one or more of the conduits 254.
  • the fluid flow 404 e.g., cooling fluid 374
  • FIG. 3 is a schematic of an embodiment of the combined cycle system 10 of FIG. 1, illustrating an embodiment of the gas capture system 20 of the DAC system 18 having a solvent-based gas capture system 500.
  • the solvent-based gas capture system 500 may use one or more solvents for capturing the undesirable gases.
  • Example solvents include monoethanolamine (MEA), diglycolamine (DGA). advanced amine solvents, amino acid salts, carbonate solvents, aqueous ammonia, immiscible liquids, and ionic liquids.
  • the solvent-based gas capture system 500 uses one or more heated fluids 502 from the steam turbine system 14, the steam generation system 16, and/or the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140).
  • the heated fluids 502 may include steam and/or heated water 501, 503 from the steam turbine system 14 and/or the steam generation system 16.
  • the heated fluids 502 may include heated gas and/or heated liquid (e.g., thermal fluid 34) from the thermodynamic cycle 24 and/or the thermal storage system 140 of the via the WHR system 22.
  • the thermodynamic cycle 24 is driven by waste heat recovered from the thermal power systems 28 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54), and extracts waste heat as the thermal fluid 34 for use in the one or more gas capture systems 20 (e.g.. solvent-based gas capture system 500) of the DAC system 18.
  • the gas capture system 20 may be configured to route the heated fluid 502 (e.g., steam and/or heated water 501, 503) from the steam turbine system 14 and/or the steam generation system 16 to the gas capture system 20 (e.g., solvent-based gas capture system 500), wherein the steam may be high-pressure steam, intermediate-pressure steam, and/or low-pressure steam extracted from one or more sections of the steam generation system 16 and/or one or more of the steam turbines 80, 82, and 84 of the steam turbine system 14.
  • the heated fluid 502 e.g., steam and/or heated water 501, 503
  • the gas capture system 20 e.g., solvent-based gas capture system 500
  • the steam may be high-pressure steam, intermediate-pressure steam, and/or low-pressure steam extracted from one or more sections of the steam generation system 16 and/or one or more of the steam turbines 80, 82, and 84 of the steam turbine system 14.
  • the heated fluid 502 may be supplied by the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140) to the gas capture system 20 (e.g., solvent-based gas capture system 500).
  • the solvent-based gas capture system 500 includes an absorber 504 (e.g., absorber column), a stripper 506 (e.g., stripper column), a gas circuit 508 (e.g., gas treatment circuit), a solvent circuit 510 (e.g., fluid absorbent circuit), and one or more heated fluid circuits 512.
  • Each of the gas circuit 508, the solvent circuit 510, and the heated fluid circuits 512 includes one or more fluid conduits or lines, fluid manifolds, fluid splitters, fluid combiners, fluid mixing chambers, fluid valves, internal fluid paths through components, or any combination thereof.
  • the gas circuit 508 is configured to route the air 190 (or any other gas flow having undesirable gases) through the absorber 504, while the solvent circuit 456 is configured to route a solvent flow through the absorber 504 and the stripper 506.
  • the gas circuit 508 includes a gas path 514 extending toward the absorber 504 between the absorber 504 and the WHR system 22 and/or the steam generation system 16, a gas path 516 extending upwardly through the absorber 504, and a gas path 518 extending away from the absorber 504.
  • the solvent circuit 510 extends through the absorber 504 and the stripper 506 in a loop, including a solvent path 520 extending downwardly through the absorber 504, a solvent path 522 extending from the absorber 504 to the stripper 506, a solvent path 524 extending downwardly through the stripper 506, and a solvent path 526 extending from the stripper 506 to the absorber 504.
  • the heated fluid circuits 512 extend between the stripper 506 and one or more heated fluid sources 528 to support operation of the stripper 506 using the heated fluid 502.
  • the heated fluid circuits 512 may be configured to extract the heated fluid 502 at a pressure and a temperature suitable for transferring heat to the stripper 506 to reduce or eliminate a need for separate heat sources for the stripper 506.
  • the heated fluid circuits 512 may be configured to provide a high-pressure steam, an intermediate-pressure steam, and/or a low-pressure steam (e.g.. steam 501. 503) to the stripper 506 from the steam turbine system 14 and/or the steam generation system 16 as the heated fluid sources 528.
  • the heated fluid sources 528 include the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140) as a source of the heated fluid 502 (e.g., thermal fluid 34).
  • the heated fluid circuits 512 may include any number and configurations of heated fluid flow paths (e.g., conduits), connection locations, and control features to provide suitable heated fluid 502 to the stripper 506.
  • the heated fluid circuits 512 may fluidly and mechanically couple to the heated fluid sources 528 at one or more heated fluid extraction locations 530 (e.g., extraction ports or connections).
  • the heated fluid extraction locations 530 may be disposed at one or more locations along the thermodynamic cycle 24.
  • the heated fluid extraction locations 530 may include one or more heated water and/or steam extraction locations 530 at the steam turbine system 14 and/or the steam generation system 16, such as locations at, upstream of, downstream of, and/or between: the sections (e.g., high-pressure, intermediate-pressure, and low-pressure sections) of the steam generation system 16 and the steam turbines 80, 82, and 84.
  • the heated fluid circuits 512 may fluidly and mechanically couple to the stripper 506 at one or more heated fluid injection locations 532 (e.g., injection ports or connections).
  • the heated fluid injection locations 532 may be disposed at, upstream of, downstream of. and/or between components of the stripper 506.
  • the solvent-based gas capture system 500 may have one or more of the heated fluid circuits 512 with any combination of the heated fluid extraction locations 530 and the heated fluid injection locations 532.
  • the heated fluid circuits 512 may be independent circuits (e.g., separate heated fluid paths or conduits) or interconnected circuits (e.g., fluidly coupled heated fluid paths or conduits) having one or more common conduits, wherein the heated fluid circuits 512 may include one or more valves 534 coupled to the controller 220 for selective control of the heated fluid flows to the stripper 506.
  • the heated fluid circuits 512 include one or more heated fluid circuit 536 between the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140) and the stripper 506.
  • the one or more heated fluid circuits 536 are fluidly and mechanically coupled to the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140) at one or more heated fluid extraction locations 530, and the one or more heated fluid circuits 536 are fluidly and mechanically coupled to the stripper 506 at one or more heated fluid injection locations 532 (e.g., 540, 542, 544, and 546).
  • the heated fluid circuits 512 may include one or more heated water and/or steam circuits extending between the stripper 506 and one or more of the sections (e.g., high-pressure, intermediate-pressure, and low-pressure sections) of the steam generation system 16, one or more heated water and/or steam circuits extending between the stripper 506 and one or more of the steam turbines 80, 82, and 84 of the steam turbine system 14, or any combination thereof.
  • the heated fluid extraction locations 530 may include a plurality of different locations
  • the heated fluid injection locations 532 e.g., 540, 542, 544, and 546) may include a plurality' of different locations.
  • the heated fluid circuits 512 may include one or more common heated fluid extraction locations 530, one or more common heated fluid injection locations 532 (e.g., 540, 542, 544, and 546), or any combination thereof.
  • each of the heated fluid circuits 512 may selectively couple to the stripper 506 at any one or more of the heated fluid injection locations 532 (e.g., 540, 542, 544, and 546) using conduits, valves 534, manifolds, and other flow controls.
  • the heated fluid circuits 512 are configured to provide the heated fluid 502 to the stripper 506 at a temperature, a pressure, and a flow rate at least partially controlled by the valves 534 (e.g., controlled via the controller 220 and feedback from sensors 222) along the respective heated fluid circuits 512. Additional details of the heated fluid circuits 512 and the heated fluid supply to the stripper 506 will be discussed below.
  • the absorber 504 includes a plurality of absorber sections 560 disposed inside of a vessel or enclosure 562, wherein the enclosure 562 includes a gas inlet 564, a gas outlet 566, a solvent inlet 568, and a solvent outlet 570.
  • the enclosure 562 has a top portion 572, a bottom portion 574, and an intermediate portion 576 disposed axially between the top and bottom portions 572 and 574 relative to a central axis 578 of the enclosure 562.
  • the top portion 572 includes a top plate or cover 580 having the gas outlet 566 coaxial with the central axis 578. However, the gas outlet 566 may be disposed offset from the central axis 578 or at other locations along the top portions 572.
  • the intermediate portion 576 includes a sidewall 582 extending about the central axis 578.
  • the sidewall 582 may be an annular sidewall, a square shaped sidewall, a rectangular sidewall, or any other suitable shape that extends around the central axis 578.
  • the gas outlet 566 may be disposed in the sidewall 582 along the top portion 572.
  • the solvent inlet 568 may be disposed along the top plate or cover 580 or the sidewall 582 in the top portion 572.
  • the bottom portion 574 may include a base plate 584 below the gas inlet 564 and the solvent outlet 570. In the illustrated embodiment, the gas inlet 564 and the solvent outlet 570 are disposed in the sidewall 582 along the bottom portion 574.
  • the gas inlet 564 and/or the solvent outlet 570 may be disposed in the base plate 584 in the bottom portion 574.
  • the gas inlet 564 may include a plurality of gas inlets and/or the solvent outlet 570 may include a plurality of solvent outlets.
  • the plurality of absorber sections 560 within an interior volume 586 of the enclosure 562 may include any number and type of absorber sections 560, such as absorber sections 588, 590, 592, 594, 596, and 598, which may include any configuration of packings, support trays or screens, wire meshes, solvent distributors, or any combination thereof.
  • each packing may include a plurality of beads, balls, or mixture inducing structures, which are configured to facilitate mixing between a gas flow and a solvent flow in the absorber 504.
  • Each support tray or screen may include a wire mesh, a plate having a plurality of openings, or another suitable structure that holds the packing in position while permitting fluid flow of gas and solvent through the support tray or screen in opposite directions through the absorber 504.
  • Each solvent distributor may include a plurality' of solvent nozzles configured to distribute solvent across the interior volume 586.
  • the absorber sections 588, 592, 596, and 598 include wire meshes, while the absorber sections 590 and 594 include packings, support trays or screens, and solvent distributors.
  • the absorber sections 560 e.g., 588, 590, 592, 594, 596, and 598) are not limited to the illustrated configuration.
  • the absorber 504 is configured to create a crossflow or opposing flows of a gas 600 (e.g., air 190 and/or other gas) along the gas path 516 and a gas lean solvent 602 along the solvent path 520 within the interior volume 586, thereby facilitating gas absorption of certain undesirable gases (e.g., CO2) from the gas 600 into the gas lean solvent 602.
  • a gas 600 e.g., air 190 and/or other gas
  • gases e.g., CO2
  • the gas 600 enters the absorber 504 through the gas inlet 564, and the gas 600 flows upwardly through the interior volume 586 of the absorber 504.
  • the gas 600 entering the absorber 504 through the gas inlet 564 may form bubbles of the gas 600 that rise upwardly through the gas lean solvent 602 within the interior volume 586.
  • the gas 600 then passes through each subsequent absorber section 560 (e.g., 588, 590. 592, 594, 596. and 598).
  • the solvent-based gas capture system 500 supplies the gas lean solvent 602 into the interior volume 586 using one or more solvent distributors, such as a solvent distribution manifold, solvent nozzles, or a grid of solvent injectors.
  • the solvent-based gas capture system 500 may supply the gas lean solvent 602 through the illustrated solvent inlet 568, or any number or arrangement of solvent inlets 568, at positions directly at, above, and/or below the absorber sections 560.
  • the gas lean solvent 602 then flows downwardly through the interior volume 586 through each subsequent absorber section 560.
  • various mixing structures e.g., packings, wire meshes, support trays, etc.
  • the gas lean solvent 602 may be configured to absorb carbon dioxide (CO2) or other undesirable gases as discussed in detail above.
  • CO2 carbon dioxide
  • heat is generated within the absorber 504, thereby raising the temperature of the solvent within the absorber 504.
  • a thermal control system 604 may be coupled to the absorber 504 to control the temperatures and improve the efficiency of the absorption process.
  • the thermal control system 604 may include a cooling circuit 606 coupled to the absorber 504, wherein the cooling circuit 606 includes a heat exchanger 608 (e.g., cooler) and a pump 610.
  • the pump 610 is configured to circulate solvent through the heat exchanger 608 to cool the solvent by transferring heat away from the solvent to a cooling fluid, such as water or another coolant. Any number or configuration of thermal control systems 604 may be implemented in the absorber 504.
  • the absorber 504 also includes a water wash system 612 having a heat exchanger 614 (e.g., cooler) and a pump 616 disposed along a water wash circuit 618.
  • the absorber section 594, 596, and/or 598 may be configured to assist with the water wash process of the water wash system 612, while the absorber sections 588, 590, and 592 help to enhance mixing between the gas 600 and the gas lean solvent 602 to increase absorption of the undesirable gases.
  • the absorber section 594, 596, and/or 598 may be configured to help distribute water across the absorber 504 in the top portion 572 for removing any dissolved solvent in the gas 600 flowing upwardly through the absorber 504.
  • the water wash system 612 may be eliminated or moved downstream from the absorber 504.
  • the absorber 504 discharges a gas rich solvent 620 at the bottom portion 574 through the solvent outlet 570, and the absorber 504 discharges the treated gas 622 at the top portion 572 through the gas outlet 566.
  • the treated gas 622 may be substantially free or stripped of one or more undesirable gases (e g., CO2).
  • the gas rich solvent 620 may have absorbed the one or more undesirable gases (e g., CO2).
  • the gas rich solvent 620 may be described as a CO2 rich solvent (or other gas rich solvent depending on the undesirable gas), while the gas lean solvent 602 may be described as a CO2 lean solvent (or other gas lean solvent depending on the undesirable gas and the particular gas absorption occurring in the absorber 504).
  • the gas 600 may be described as a CO2 containing or rich gas (or other containing or rich gas depending on the undesirable gas), while the treated gas 622 may be described as a CO2 reduced, lean, or free gas (or other reduced, lean, or free gas depending on the undesirable gas and the particular gas absorption occurring in the absorber 504).
  • the gas absorption discussed herein is intended to cover any one or more of the undesirable gases described herein, or any other regulated or greenhouse gases.
  • the gas circuit 508 may include one or more components upstream from the absorber 504.
  • the gas circuit 508 may include one or more compressors 210 configured to compressor the air 190 upstream from the absorber 504.
  • the gas circuit 508 may include a gas cooler or gas cooling system, such as a direct contact cooler (DCC) 624, disposed along the gas path 514 upstream from the absorber 504.
  • DCC direct contact cooler
  • the DCC 624 may be downsized or eliminated in the solventbased gas capture system 500.
  • the DCC 624 may include a cooling enclosure 626 that houses a wire mesh 628 and a cooling fluid distributor 630, wherein the cooling fluid distributor 630 includes a plurality of fluid nozzles 632.
  • the DCC 624 also may include a cooling fluid circuit 634 having a pump 636 and a heat exchanger 638 (e.g., cooler), wherein the cooling fluid circuit 634 is coupled to the cooling fluid distributor 630 above the wire mesh 628 and a bottom portion of the enclosure 626 below the wire mesh 628.
  • the pump 636 is configured to circulate a cooling fluid (e.g., water or other liquid) through the DCC 624, while the heat exchanger 638 is configured to cool the cooling fluid by transferring heat away from the cooling fluid to another working fluid.
  • a cooling fluid e.g., water or other liquid
  • the plurality of fluid nozzles 632 distribute the cooling fluid across an interior volume of the enclosure 626 (e.g., cooling fluid dispersion), while the DCC 624 routes a gas flow from a gas inlet 640 to a gas outlet 642 as indicated by arrow 644.
  • the cooling fluid dispersion directly contacts and cools the gas flow (e.g., air 190 and/or other gas).
  • the gas circuit 508 also includes one or more compressors and/or fans 646 configured to boost a pressure and/or flow rate of the gas flow (e.g., air 190 and/or other gas) supplied to the absorber 504.
  • the solvent-based gas capture system 500 also may include a plurality of components along the solvent circuit 510 between the absorber 504 and the stripper 506.
  • the solvent circuit 510 includes a pump 648, a heat exchanger 650. and a heat exchanger 704 along the solvent path 522 from the absorber 504 to the stripper 506, and the solvent circuit 510 includes a pump 652, the heat exchanger 650, a heat exchanger 654, and a filter 656 along the solvent path 526 from the stripper 506 to the absorber 504.
  • the pump 648 is configured to pump the gas rich solvent 620 along the solvent path 522 through the heat exchanger 650 and the heat exchanger 704 to the stripper 506, while the pump 652 is configured to pump the gas lean solvent 602 along the solvent path 526 through the heat exchangers 654 and 656 and the filter 656 to the absorber 504.
  • the heat exchanger 650 is configured to transfer heat away from the gas lean solvent 602 in the solvent path 526 to the gas rich solvent 620 in the solvent path 522, thereby cooling the gas lean solvent 602 and heating the gas rich solvent 620.
  • the heat exchanger 704 is configured to transfer heat from the heated fluid 502 in a heated fluid circuit 702 to the gas rich solvent 620 in the solvent path 522, thereby heating the gas rich solvent 620.
  • the heat exchanger 654 is configured to cool the gas lean solvent 602 by transferring heat away from the gas lean solvent 602 to a coolant flow (e.g., water or other liquid coolant), thereby providing a cooled gas lean solvent 602 for supply to the absorber 504.
  • the filter 656 is configured to filter and/or clean the gas lean solvent 602 for use in the absorber 504.
  • the solvent circuit 510 may include additional components (e.g., heat exchangers, filters, valves, etc.) and/or exclude one or more of the illustrated components.
  • the stripper 506 processes the gas rich solvent 620 as discussed below.
  • the stripper 506 includes a plurality of stripper sections 658 disposed inside of a vessel or enclosure 660, wherein the enclosure 660 includes a solvent inlet 662, a solvent outlet 664, and a gas outlet 666.
  • the enclosure 660 has a top portion 668, a bottom portion 670, and an intermediate portion 672 disposed axially between the top and bottom portions 668 and 670 relative to a central axis 674 of the enclosure 660.
  • the top portion 668 includes a top plate or cover 676 having the gas outlet 666 coaxial with the central axis 674. However, the gas outlet 666 may be disposed offset from the central axis 674 or at other locations along the top portion 668.
  • the intermediate portion 672 includes a sidewall 678 extending about the central axis 674.
  • the sidewall 678 may be an annular sidewall, a square shaped sidewall, a rectangular sidewall, or any other suitable shape that extends around the central axis 674.
  • the gas outlet 666 may be disposed in the sidewall 678 along the top portion 668.
  • the solvent inlet 662 may be disposed along the top portion 668 or the intermediate portion 672.
  • the bottom portion 670 may include a base plate 680 below the solvent outlet 664.
  • the solvent outlet 664 is disposed in the sidewall 678 along the bottom portion 670.
  • the solvent outlet 664 may be disposed in the base plate 680 in the bottom portion 670.
  • the plurality of stripper sections 658 within an interior volume 682 of the enclosure 660 may include any number and type of stripper sections 658, such as stripper sections 684, 686, 688, 690, and 692, which may include any configuration of packings, support trays or screens, wire meshes, solvent distributors having nozzles, steam distributors having nozzles, or any combination thereof.
  • each packing may include a plurality of beads, balls, or mixture inducing structures, which are configured to facilitate mixing between flows of a solvent flow (e.g., gas rich solvent 620) and a steam 694 in the stripper 506.
  • Each support tray or screen may include a wire mesh, a plate having a plurality 7 of openings, or another suitable structure that holds the packing in position while permitting fluid flow of the solvent (e.g., gas rich solvent 620) and the steam 694 through the support tray or screen.
  • Each solvent distributor may include a plurality of solvent nozzles configured to distribute solvent across the interior volume 682.
  • Each steam distributor may include a plurality of fluid nozzles configured to distribute steam 694 across the interior volume 682.
  • the stripper sections 686, 688. and 692 include wire meshes
  • the stripper section 684 includes a packing and a support tray or screen
  • the stripper section 690 includes a barrier plate or divider plate having one or more openings.
  • the stripper sections 658 are not limited to the illustrated configuration.
  • the stripper 506 is configured to strip the undesirable gases from the gas rich solvent 620 using the heated fluid 502 supplied by the heated fluid circuits 512 from one or more of the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140), the steam turbine system 14, the steam generation system 16, another waste heat recovery 7 system of the combined cycle system 10, or a combination thereof.
  • the heated fluid circuits 512 are coupled to various heated fluid extraction location 530 and heated fluid injection locations 532 (e.g.. 540, 542, 544. and 546) to provide heat in the form of the heated fluid 502 for supporting the stripper 506.
  • Each of these heated fluid circuits 512 may be configured to transfer heat to the solvent in the stripper 506 by direct heat transfer (e.g., direct injection into the solvent), indirect heat transfer (e.g., via a heat exchanger), or any combination thereof.
  • the controller 220 is configured to selectively control (e.g., open and close) the valves 534 to control the respective flows of heated fluid 502 through the heated fluid circuits 512 to the stripper 506.
  • the heated fluid circuits 512 include heated fluid circuits (or circuit portions) 696, 698, 700, and 702 coupled to the respective heated fluid injection locations 532 (e.g., 540, 542, 544, and 546).
  • the heated fluid circuits 512 are coupled to the intermediate portion 672 of the enclosure 660 at the respective heated fluid injection locations 532 (e.g., 542 and 544), which are located between the stripper sections 686 and 688.
  • the heated fluid circuits 698 and 700 may be coupled to the stripper 506 at any suitable heated fluid injection locations 532, which may be the same or different between the heated fluid circuits 698 and 700.
  • the heated fluid injection locations 532 e.g.. 542 and 544 may be disposed directly at. above, and/or below one or more of the stripper sections 658.
  • the heated fluid injection locations 532 e.g., 542 and 544) may include fluid distributors having a plurality' of fluid nozzles configured to distribute the heated fluid 502 across the interior volume 682 of the stripper 506.
  • the stripper 506 may be coupled to or include one or more additional components, such as a thermal control system 706 and a moisture removal system 708.
  • the thermal control system 706 may be coupled to any portion of the stripper 506, such as at the bottom portion 670.
  • the thermal control system 706 may include a solvent recirculation circuit 710 having a reboiler 712 configured to heat and boil the solvent for recirculation into the stripper 506.
  • the reboiler 712 is coupled to at least one of the heated fluid circuits 512 (e.g.. 696) as a heat source for heating and boiling the solvent, rather than relying on an independent or separate heat source.
  • the reboiler 712 may include one or more additional heat sources, such as an electric heater, a combustor or furnace, a steam generator, or other heat sources, for heating the solvent.
  • the additional heat sources may be used when steam is unavailable and/or insufficient to provide the desired heating in the reboiler 712.
  • the heated fluid circuits 512 may be the primary 7 source of heat to support the reboiler 712.
  • at least one of the heated fluid circuits 512 e.g., 696 supplies the heated fluid 502 into the reboiler 712 at an inlet 714 (e.g., the heated fluid injection location 540).
  • the reboiler 712 discharges water and/or steam at an outlet 716.
  • the discharged water and/or steam flows through a return circuit 718 from the reboiler 712 to the heated fluid source 528 (e.g., WHR system 22, including the thermodynamic cycle 24 and/or the thermal storage system 140).
  • the return circuit 718 may include a fluid treatment unit (FTU) 720 configured to treat the heated fluid 502 prior to return to the heated fluid source 528.
  • FTU fluid treatment unit
  • the FTU 720 may include a condenser configured to condense steam and/or other liquid vapor into a condensate, a particulate filter, a descaling unit, an ultraviolet (UV) treatment unit, or any combination thereof.
  • the return circuit 718 is coupled to a pump 722, which is configured to pump the heated fluid 502 back to the heated fluid source 528.
  • the heated fluid circuit 512 (e.g., 696) is coupled to the reboiler 712, any one or more of the heated fluid circuits 512 (e.g., 696, 698, 700, and 702) may be coupled to the reboiler 712 to provide the heated fluid 502 as a source of heat for heating and boiling the solvent in the stripper 506.
  • At least one of the heated fluid circuits 512 supplies the heated fluid 502 into the heated fluid injection location 544 at the heat exchanger 704 disposed along the solvent circuit 510, thereby heating the gas rich solvent 620 between the absorber 504 and the stripper 506.
  • the heat exchanger 704 may be disposed between the heat exchanger 650 and the solvent inlet 662 into the stripper 506.
  • the heated fluid 502 may be directly injected into the gas rich solvent 620, such that the heated fluid 502 mixes with and directly transfers heat to the gas rich solvent 602.
  • the heat exchanger 704 provides indirect heat transfer between the heated fluid 502 and the gas rich solvent 602, and thus the heated fluid 502 may be recirculated back to the heated fluid source 528 along a return circuit (e.g., return circuit 718).
  • a return circuit e.g., return circuit 718
  • the moisture removal system 708 may include a condenser circuit 724 having a condenser 726, wherein the condenser circuit 724 is coupled to the gas outlet 666 and a return inlet 728.
  • the condenser 726 is configured to cool and condense any steam and solvent vapor present in the captured gas 204 discharged from the stripper 506, thereby outputting water or condensate 730, the captured gas 204 substantially free of water content and solvent vapor, and solvent vapor for return to the stripper 506 via the return inlet 728.
  • the condenser 726 includes a heat exchanger (e.g., cooler) configured to transfer heat away from the captured gas 204.
  • the moisture removal system 708 is coupled to the top portion 668 of the enclosure 660. However, the moisture removal system 708 may be disposed at any suitable location to condense any steam and solvent vapor present in the captured gas 204.
  • the captured gas 204 also may be compressed in the compression system 206 and routed to a storage and/or pipeline 208 as discussed above.
  • the controller 220 is configured to monitor the sensors 222 and control operation of the solvent-based gas capture system 500, using the heated fluid 502 supplied through the heated fluid circuits 512 to support the stripper 506.
  • the controller 220 may selectively control the valves 534 to supply the heated fluid 502 through one or more of the heated fluid circuits 512 depending on the conditions of the heated fluid 502, the temperature of solvent in the stripper 506, the temperature of solvent in the reboiler 712, the operating conditions of the combined cycle system 10 (e g., startup mode, steady state mode, shutdown mode, full load mode, and/or part load mode), the percentage of undesirable gases in the air 190 and/or other gas being treated, the flow rate of the gas lean solvent 602, the flow rate of the gas rich solvent 620, the flow rate of the gas 600, or any combination thereof.
  • the controller 220 may selectively control the valves 534 to supply the heated fluid 502 through one or more of the heated fluid circuits 512 depending on the conditions of the heated fluid 502, the temperature of solvent in
  • the controller 220 may be configured to control the one or more additional heat sources (e.g., electric heaters, furnaces, etc.) and/or the thermal storage system 140 to provide heat to support the stripper 506.
  • the controller 220 may be configured to control the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140). the steam turbine system 14, the steam generation system 16, the valves 534. or any combination thereof, to provide the heated fluid 502 to the stripper 506.
  • the controller 220 may be configured to control mixing of the heated fluid 502 from the various heated fluid extraction location 530, thereby providing a desired temperature and pressure of heated fluid 502 to support the stripper 506.
  • the solvent-based gas capture system 500 may be configured to selectively use the heated fluid 502 in any manner from the WHR system 22 (e.g., thermodynamic cycle 24 and/or the thermal storage system 140), the steam turbine system 14, the steam generation system 16, or any combination thereof.
  • the heated fluid 502 may include a heated water, steam, a solvent (e.g., same solvent used in the solvent-based gas capture system 500), a supercritical fluid (e.g., same or different supercritical fluid used in the thermodynamic cycle 24), or any combination thereof.
  • a solvent e.g., same solvent used in the solvent-based gas capture system 500
  • a supercritical fluid e.g., same or different supercritical fluid used in the thermodynamic cycle 24
  • FIG. 4 is a schematic of an embodiment of the combined cycle system 10 of FIG. 1, illustrating the heat source 26 of the power system 12 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) coupled to the thermodynamic cycle 24 of the WHR system 22 along a flow path 750 of the thermal fluid 30 (e.g., along the fluid circuit 110), wherein the thermodynamic cycle 24 and/or the thermal storage system 140 are configured to provide the thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18.
  • the gas capture systems 20 may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof.
  • the gas capture systems 20 may include the sorbent-based gas capture system 250 of FIG.
  • thermodynamic cycle 24 e.g., the thermodynamic cycle 24 and the thermal storage system 140
  • FIG. 4 illustrates additional details of the thermodynamic cycle 24 of the WHR system 22 that may be used in FIGS. 1-3.
  • the thermodynamic cycle 24 includes a fluid circuit or loop 752 that intersects the flow path 750 at a primary heat exchanger 754 of the WHR system 22.
  • the primary heat exchanger 754 is configured to exchange heat from the thermal fluid 30 along the flow path 750 to a working fluid 756 (e.g.. working fluid 32) in the fluid circuit 752, thereby recovering waste heat from the thermal fluid 30 to heat the working fluid 756 in the thermodynamic cycle 24.
  • the w orking fluid 756 may include one or more supercritical fluids (SCFs), inert gases such as noble gases, organic working fluids, or any combination thereof.
  • the SCF may include a supercritical carbon dioxide (sCCh) or sCCh blend having one or more dopants.
  • the noble gases may include helium (He), xenon (Xe), or a combination thereof (e.g., He-Xe mixture).
  • the inert gas may include nitrogen.
  • the organic working fluids may include hydrocarbons (HCs), fluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof.
  • the w orking fluid 756 may include the SCF, such as the sCCh or sCCh blend having one or more dopants.
  • the dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (CeFe), titanium tetrachloride (TiCk). or any combination of dopants.
  • the sCCh blend may have 5% to 20%mol dopants to increase the supercritical temperature of the SCO2.
  • the dopants may increase the critical temperature of the SCO2 to about 70 to 100 degrees Celsius without a notable drop in efficiency.
  • the SCO2 blend may increase the amount of w aste heat quantity by condensing the SCO2 blend at a higher temperature.
  • all or substantially all of the waste heat rejected from the thermodynamic cycle 24 is available for use with the DAC system 18 as the thermal fluid 34. If the heat exceeds the thermal needs of the DAC system 18. then the excess heat may be stored in the thermal storage system 140 as discussed in detail above.
  • the thermodynamic cycle 24 has a plurality of components 751 including, for example, a compressor 758, a recuperator 760, the primary heat exchanger 754. a turbine 762, a waste heat recover ⁇ ' (WHR) heat exchanger 764, and a pre-cool er 766 arranged along the fluid circuit 752. wherein the fluid circuit 752 includes a plurality of fluid lines or conduits 768, 770, 772. 774, 776, 778, and 780 and internal flow paths through the plurality of components 751.
  • the fluid circuit 752 includes a plurality of fluid lines or conduits 768, 770, 772. 774, 776, 778, and 780 and internal flow paths through the plurality of components 751.
  • the components 751 also may include a plurality of valves and sensors disposed at, upstream from, and/or downstream from each of the components 751, wherein the controller 220 is communicatively coupled to the valves, the sensors, and the components 751 to control the thermodynamic cycle 24.
  • the working fluid 756 passes through the fluid circuit 752 sequentially through the compressor 758, the fluid conduit 768, the recuperator 760, the fluid conduit 770, the primary heat exchanger 754, the fluid conduit 772, the turbine 762, the fluid conduit 774, the recuperator 760, the fluid conduit 776, the WHR heat exchanger 764, the fluid conduit 778, the pre-cooler 766, the fluid conduit 780, and then back to the compressor 758.
  • the primary heat exchanger 754 recovers heat from the thermal fluid 30 to heat the working fluid 756.
  • the WHR heat exchanger 764 rejects waste heat (i.e. heat that would otherwise be rejected to the environment in the precooler 766) from the working fluid 756 as a heat source to provide the thermal fluid 34 from the thermodynamic cycle 24 to the gas capture systems 20 of the DAC system 18.
  • the compressor 758 is configured to compress the working fluid 756 (e.g., SCF) and supply the compressed working fluid 756 to the recuperator 760 along the fluid conduit 768.
  • the compressor 758 may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft, which is driven to rotate by the turbine 762 via a shaft 782.
  • the recuperator 760 includes a heat exchanger having a first internal flow path 784 between the fluid conduits 768 and 770 and a second internal fluid path 786 between the fluid conduits 774 and 776, wherein the recuperator 760 is configured to transfer heat from the working fluid 756 in the second internal flow path 786 to the working fluid 756 in the first internal flow path 784.
  • the recuperator 760 increases a temperature of the working fluid 756 (e.g., heated working fluid) supplied through the fluid conduit 770 to the primary heat exchanger 754, and decreases a temperature of the working fluid 756 (e.g., cooled working fluid) supplied through the fluid conduit 776 to the WHR heat exchanger 764.
  • the temperature of the cooled working fluid 756 may approximately 100 to 150 degrees Celsius. 100 to 140 degrees Celsius, or 100 to 130 degrees Celsius.
  • the primary’ heat exchanger 754 of the thermodynamic cycle 24 includes a first internal flow path 788 between the fluid conduits 770 and 772 of the fluid circuit 752 and a second internal fluid path 790 between fluid conduits 792 and 794 of the flow path 750, wherein the primary’ heat exchanger 754 is configured to transfer heat from the thermal fluid 30 in the second internal flow path 790 to the working fluid 756 in the first internal flow path 788.
  • the primary heat exchanger 754 increases a temperature of the working fluid 756 (e.g., heated working fluid) supplied through the fluid conduit 772 to the turbine 762, and decreases a temperature of the thermal fluid 30 (e.g., cooled thermal fluid) discharged through the fluid conduit 794.
  • the primary heat exchanger 754 may be configured to increase the temperature of the working fluid 756 to a temperature of approximately 550 to 700 degrees Celsius, or at least equal to or greater than approximately 500, 510, 520, 530, 540, 550, 560, 570, 580, 590, 600, 610, 620, 630, 640, or 650 degrees Celsius.
  • the heated working fluid 756 then expands through the turbine 762 as discussed in further detail below.
  • the primary' heat exchanger 754 may receive the thermal fluid 30 (e.g., hot or heated thermal fluid) at a temperature of approximately 570 to 720 degrees Celsius and output the thermal fluid 30 (e.g., cold or cooled thermal fluid) at a temperature range of approximately 50 to 100 degrees Celsius, such as temperatures of approximately 50, 60, 70, 80, 90, or 100 plus or minus 1, 2, 3, 4 or 5 degrees Celsius.
  • the thermal fluid 30 then passes through the heat source 26 for reheating by one or more of the thermal power systems 28 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54).
  • the thermal power systems 28 e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54.
  • the turbine 762 receives the heated working fluid 756 from the primary’ heat exchanger 754.
  • the turbine 762 may include one or more turbines and/or turbine stages.
  • the heated working fluid 756 expands through the turbine 762, thereby driving rotation of turbine blades and a turbine shaft of the turbine 762 to drive rotation of the shaft 782 coupled to the compressor 758.
  • the turbine 762 also may be coupled to a load 798, such as a mechanical load and/or an electrical generator.
  • the load 798 is a primary function of the thermodynamic cycle 24, such that the thermodynamic cycle 24 generates mechanical and/or electrical power using heat from the heat source 26.
  • the working fluid 756 decreases in temperature and decreases in pressure upstream from the recuperator 760. However, the working fluid 756 still contains excess heat.
  • the working fluid 756 from the turbine 762 then flows through the recuperator 760, which cools the working fluid 756 (e.g., cooled working fluid) upstream from the WHR heat exchanger 764 as discussed above.
  • the temperature of the cooled working fluid 756 may be approximately 100 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, 130 to 150 degrees Celsius, or 100 to 130 degrees Celsius when reaching the WHR heat exchanger 764.
  • the WHR heat exchanger 764 is configured to extract or reject waste heat from the working fluid 756 to generate the thermal fluid 34, which is supplied to one or more gas capture systems 20 of the DAC system 18 via one or more fluid circuits 800 (e.g., fluid circuit 130).
  • Each of the fluid circuits 800 may include a closed loop fluid circuit between the WHR heat exchanger 764 and one of the gas capture systems 20, wherein the fluid circuits 800 may include fluid conduit, valves, sensors, flow regulators, and other flow control equipment to control the flow of the thermal fluid 34 via the controller 220.
  • the one or more fluid circuits 800 (e.g., fluid circuit 130) also couple to the thermal storage system 140 via the fluid circuit 150 as discussed in detail above.
  • the WHR heat exchanger 764 includes a first internal flow path 802 between the fluid conduits 776 and 778 of the fluid circuit 752 and a second internal fluid path 804 of the fluid circuit 800 coupled to the one or more gas capture systems 20, wherein the WHR heat exchanger 764 is configured to transfer heat from the working fluid 756 in the first internal flow path 802 to the thermal fluid 34 in the second internal flow path 804.
  • the WHR heat exchanger 764 increases a temperature of the thermal fluid 34 supplied through the fluid circuit 800 to the gas capture systems 20, and decreases a temperature of the working fluid 756 (e.g., cooled working fluid) supplied through the fluid conduit 778 to the pre-cool er 766.
  • the WHR heat exchanger 764 may be configured to increase the temperature of the thermal fluid 34 to a temperature of approximately 100 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, 130 to 150 degrees Celsius, 100 to 130 degrees Celsius, or 110 to 130 degrees Celsius, or at least equal to or greater than approximately 100, 110, 120, 130, 140, or 150 degrees Celsius plus or minus 5 degrees Celsius. Additionally, the WHR heat exchanger 764 may be configured to decrease the temperature of the working fluid 756 to a temperature of approximately 50 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or betw een approximately 40 to 60 degrees Celsius.
  • the pre-cooler 766 may include one or more heat exchangers configured to transfer heat from the working fluid 756 to the environment through an appropriate cooling fluid (e.g., river water or ambient air), thereby reducing a temperature of the working fluid 756 upstream of the compressor 758.
  • the pre-cooler 766 may be configured to decrease the temperature of the working fluid 756 to a temperature of approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or a temperature between 30 to 50 degrees Celsius or between 40 to 50 degrees Celsius.
  • the working fluid 756 then returns to the compressor 758 for another pass through the fluid circuit 752 of the thermodynamic cycle 24.
  • the primary heat exchanger 754 extracts waste heat from the thermal fluid 30 to help drive the thermodynamic cycle 24, while the WHR heat exchanger 764 rejects or extracts waste heat from the working fluid 756 (e.g., SCF) for heating the thermal fluid 34 for helping to dnve desorption (or other processes) in the gas capture systems 20.
  • the WHR heat exchanger 764 indirectly transfers heat from the working fluid 756 to the thermal fluid 34, such that fluids 34 and 756 are separate from one another. Accordingly, the fluids 34 and 756 may be the same or different from one another.
  • the thermal fluid 34 may include, for example, water, steam, SCF, solvent (e.g., solvent used in a solvent-based gas capture system), or any other suitable heat transfer fluid.
  • the WHR heat exchanger 764 may be configured to transfer or circulate a portion of the working fluid 756 through the fluid circuit 800 between the thermodynamic cycle 24 and the gas capture systems 20.
  • the WHR heat exchanger 764 may use any suitable heat transfer configuration to extract heat from the thermodynamic cycle 24 for use in the gas capture systems 20.
  • the DAC system 18 includes one or more gas capture systems 20 configured to treat the air 190 and/or other gases.
  • the air 190 is compressed by one or more compressors 210, such that the gas capture systems 20 receive a compressed air 190 for treatment.
  • the DAC system 18 is configured to capture the undesirable gases (e.g., CO2) from the air 190, and then output the treated air 191 and the captured gas 204.
  • the treated air 191 generally has a concentration of the undesirable gases (e.g., CO2) substantially less than atmospheric levels.
  • the thermal fluid 34 supports (e.g., as a heat source) at least the desorption mode in the gas capture systems 20.
  • the thermal fluid 34 may be provided to the DAC system 18 from the thermodynamic cycle 24 and/or the thermal storage system 140 depending on the heat demands in the gas capture systems 20. If excess heat cannot be used in the DAC system 18 and/or the thermal storage system 140, then the excess heat can be rejected into the atmosphere via the heat exchanger 162 of the waste heat discharge system 160.
  • FIG. 5 is a schematic of an embodiment of the combined cycle system 10 of FIG. 1, illustrating the heat source 26 of the power system 12 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) coupled to the thermodynamic cycle 24 of the WHR system 22 along a flow path 850 of the thermal fluid 30 (e.g., along the fluid circuit 110), wherein the thermodynamic cycle 24 and/or the thermal storage system 140 are configured to provide the thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18.
  • the gas capture systems 20 may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof.
  • the gas capture systems 20 may include the sorbent-based gas capture system 250 of FIG.
  • FIG. 5 illustrates additional details of the thermodynamic cycle 24 of the WHR system 22 that may be used in FIGS. 1-3.
  • the thermodynamic cycle 24 includes a fluid circuit or loop 852 that intersects the flow path 850 at a plurality of primary heat exchangers 854 of the WHR system 22.
  • Each primary heat exchanger 854 is configured to exchange heat from the thermal fluid 30 along the flow path 850 to a working fluid 856 (e.g., working fluid 32) in the fluid circuit 852, thereby transferring heat from the thermal fluid 30 to heat the working fluid 856 in the thermodynamic cycle 24.
  • the working fluid 856 may include one or more supercritical fluids (SCFs), inert gases such as noble gases, organic working fluids, or any combination thereof.
  • the SCF may include a supercritical carbon dioxide (SCO2) or SCO2 blend having one or more dopants.
  • the noble gases may include helium (He), xenon (Xe), or a combination thereof (e.g., He- Xe mixture).
  • the inert gas may include nitrogen.
  • the organic working fluids may include hydrocarbons (HCs), fluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof.
  • the working fluid 856 may include the SCF. such as the SCO2 or SCO2 blend having one or more dopants.
  • the dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (CeFe), titanium tetrachloride (TiCI i). or any combination of dopants.
  • the sCCh blend may have 5% to 20%mol dopants to increase the supercritical temperature of the SCO2.
  • the dopants may increase the critical temperature of the SCO2 to about 70 to 100 degrees Celsius without a notable drop in efficiency.
  • the SCO2 blend may increase the amount of waste heat quantity' by condensing the sCCh blend at a higher temperature. As a result, all or substantially all of the waste heat rejected from the thermodynamic cycle 24 is available for use with the DAC system 18 as the thermal fluid 34.
  • the WHR system 22 may include any number of primary heat exchangers 854, such as 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more primary heat exchangers 854.
  • the primary heat exchangers 854 include primary' heat exchangers 858 and 860.
  • the thermodynamic cycle 24 has a plurality of components 862 including, for example, one, two, or more compressors 864, waste heat recovery' (WHR) heat exchangers 866, primary' heat exchangers 854, recuperators 868 (e.g., heat exchangers), turbines 870. and pre-coolers 872 arranged along the fluid circuit 852, wherein the fluid circuit 852 includes a plurality of fluid lines or conduits 874 between and fluidly connecting the components 862.
  • the components 862 also may include a plurality' of valves and sensors disposed at, upstream from, and/or downstream from each of the components 862, wherein the controller 220 is communicatively coupled to the valves, the sensors, and the components 862 to control the thermodynamic cycle 24.
  • the one or more compressors 864 include a compressor 876
  • the WHR heat exchangers 866 include a WHR heat exchanger 878
  • the recuperators 868 include a recuperator 880
  • the turbines 870 include turbines 882 and 884
  • the pre-coolers 872 include a precooler 886.
  • the thermodynamic cycle 24 of FIG. 5 operates substantially the same as discussed above with multiple primary heat exchangers 854 (e.g., primary' heat exchangers 858 and 860) and multiple turbines 870 (e.g., turbines 882 and 884).
  • the primary’ heat exchangers 854 recover heat from the thermal fluid 30 to heat the working fluid 856, wherein the heat source 26 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) provides heat for heating the thermal fluid 30 and producing power in the turbines 870.
  • the WHR heat exchangers 866 e.g., WHR heat exchanger 878, rejects waste heat from the working fluid 856 as a heat source to provide the thermal fluid 34 from the thermodynamic cycle 24 to the gas capture systems 20 of the DAC system 18.
  • the components 862 of the thermodynamic cycle 24 are arranged along a relative high-pressure (HP) circuit portion 888 of the fluid circuit 852 downstream from the compressors 864 (e.g., compressor 876) and upstream from the turbines 870 (e.g., turbines 882 and 884), or a relatively low- pressure (LP) circuit portion 890 of the fluid circuit 852 downstream from the turbines 870 (e.g., turbines 882 and 884) and upstream from the compressors 864 (e.g., compressor 876).
  • the compressors 864 transition from the LP circuit portion 890 to the HP circuit portion 888 of the fluid circuit 852 by compressing the working fluid 856.
  • the turbines 870 transition from the HP circuit portion 888 to the LP circuit portion 890 of the fluid circuit 852 by extracting work from the working fluid 856. thereby reducing the pressure of the working fluid 856 and driving one or more loads 883 and 885 (e.g., mechanical loads and/or electrical generators) and shafts (e.g., shafts coupled to the compressors 864).
  • the loads 883 and 885 are a primary function of the thermodynamic cycle 24, such that the thermodynamic cycle 24 generates mechanical and/or electrical power using heat from the heat source 26.
  • the primary heat exchangers 858 and 860 are disposed along and fluidly couple to the fluid circuit 852 upstream from the respective turbines 882 and 884, such that the primary heat exchanger 858 is along the HP circuit portion 888 and the primary’ heat exchanger 860 is at a transition between the HP circuit portion 888 and the LP circuit portion 890 of the fluid circuit 852.
  • the recuperator 880 is disposed at an intersection 892 between the HP circuit portion 888 and the LP circuit portion 890 of the fluid circuit 852.
  • the WHR heat exchangers 866 e.g., WHR heat exchanger 878) and the pre-coolers 872 (e.g., pre-cooler 886) are disposed along and fluidly couple to the LP circuit portion 890 of the fluid circuit 852.
  • the compressors 864 are configured to compress the working fluid 856 (e.g., working fluid 32) and supply the compressed working fluid 856 to the recuperators 892 (e.g., recuperator 880).
  • the compressors 864 e.g., compressor 876) may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft, which is driven to rotate by the one or more turbines 870 (e.g., turbines 882 and 884) via one or more shafts.
  • the recuperator 880 transfers heat between the working fluid 856 along the HP circuit portion 888 (e.g.. between the compressors 864 and the turbines 870) and the LP circuit portion 890 (e.g...
  • the primary heat exchangers 854 are configured to use heat from the heat source 26 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) to provide heat to the thermodynamic cycle 24 via the thermal fluid 30.
  • the primary heat exchanger 858 transfers heat from the thermal fluid 30 along the flow path 850 (e.g., fluid circuit 110) to the working fluid 856 along the fluid circuit 852, thereby heating the working fluid 856 prior to the turbine 882.
  • the turbine 882 is driven by and expands the heated working fluid 856 from the primary heat exchanger 858, and outputs a relatively lower pressure working fluid 856 to the next primary heat exchanger 860.
  • the primary' heat exchanger 860 transfers heat from the thermal fluid 30 along the flow path 850 (e.g., fluid circuit 110) to the working fluid 856 along the fluid circuit 852, thereby heating the working fluid 856 prior to the turbine 884.
  • the turbine 884 is driven by and expands the heated working fluid 856 from the primary' heat exchanger 860, and outputs a relatively lower pressure working fluid 856 for delivery along the LP circuit portion 890 to the recuperator 880 at the intersection 892.
  • the thermodynamic cycle 24 may include any number of pairs (e.g., 1, 2, 3, 4, 5, or more) of primary heat exchangers 854 and turbines 870, wherein each pair includes at least one of the primary' heat exchangers 854 upstream from a corresponding one of the turbines 870.
  • the recuperator 880 transfers heat between the working fluid 856 along the HP circuit portion 888 and the LP circuit portion 890, thereby cooling the working fluid 856 prior to the WHR heat exchangers 866 (e g., WHR heat exchanger 878).
  • the WHR heat exchanger 878 is configured to transfer heat for cooling the working fluid 856 (e.g.. cooled working fluid) along the LP circuit portion 890 between the recuperator 880 and the pre-cooler 886, while heating the working fluid (e.g., thermal fluid 34) along the fluid circuit 130 coupled to the one or more gas capture systems 20 of the DAC system 18.
  • the WHR heat exchanger 878 may be configured to increase the temperature of the thermal fluid 34 to a temperature of approximately 100 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, 130 to 150 degrees Celsius, or 110 to 130 degrees Celsius, or at least equal to or greater than approximately 100. 110, 120, 130, 140, or 150 degrees Celsius plus or minus 5 degrees Celsius.
  • the WHR heat exchanger 878 may be configured to decrease the temperature of the working fluid 856 to a temperature of approximately 50 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or between approximately 40 to 60 degrees Celsius.
  • the pre-coolers 872 may include one or more heat exchangers configured to transfer heat from the working fluid 856 to the environment via a cooling fluid (e.g., river water or ambient air), thereby reducing a temperature of the working fluid 856 upstream of the compressors 864 (e.g., compressor 876).
  • a cooling fluid e.g., river water or ambient air
  • the pre-coolers 872 may be configured to decrease the temperature of the working fluid 856 to a temperature of approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2.
  • the working fluid 856 then returns to the compressors 864 (e.g., compressor 876) for another pass through the fluid circuit 852 of the thermodynamic cycle 24.
  • the heat source 26 e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54
  • the DAC system 18 uses waste heat extracted from the thermodynamic cycle 24 via the WHR heat exchangers 866 (e.g., WHR heat exchanger 878).
  • the WHR heat exchanger 878 is configured to extract or reject waste heat from the working fluid 856 to generate the thermal fluid 34. which is supplied to one or more gas capture systems 20 of the DAC system 18 via the fluid circuit 130.
  • the thermodynamic cycle 24 may reject the waste heat to the environment, such that the waste heat is not used for any useful purpose.
  • the thermal fluid 34 may transfer heat to the gas capture systems 20 during a desorption mode, thereby facilitating desorption of undesirable gases (e.g., CO2) from the air 190 or other gases. If the thermal fluid 34 contains excess heat beyond the needs of the DAC system 18. then the thermal storage system 140 stores the excess heat for later usage by the DAC system 18. For example, if the thermal fluid 34 contains insufficient heat to support the needs of the DAC system 18, then the thermal storage system 140 may provide the thermal fluid 34 to the DAC system 18.
  • undesirable gases e.g., CO2
  • FIG. 6 is a schematic of an embodiment of the combined cycle system 10 of FIG. 1, illustrating the heat source 26 of the power system 12 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) coupled to the thermodynamic cycle 24 of the WHR system 22 along a flow path 910 of the thermal fluid 30 (e.g., along the fluid circuit 110), wherein the thermodynamic cycle 24 and/or the thermal storage system 140 are configured to provide the thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18.
  • the gas capture systems 20 may include sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof.
  • the gas capture systems 20 may include the sorbent-based gas capture system 250 of FIG.
  • thermodynamic cycle 24 e.g., the thermodynamic cycle 24 and the thermal storage system 140
  • FIG. 6 illustrates additional details of the thermodynamic cycle 24 of the WHR system 22 that may be used in FIGS. 1-3.
  • the thermodynamic cycle 24 includes a fluid circuit or loop 912 that intersects the flow path 910 at a plurality of primary' heat exchangers 914 of the WHR system 22.
  • Each primary heat exchanger 914 is configured to exchange heat from the thermal fluid 30 along the flow path 910 to a working fluid 916 (e.g., working fluid 32) in the fluid circuit 912, thereby recovering heat from the thermal fluid 30 to heat the working fluid 916 in the thermodynamic cycle 24.
  • the working fluid 916 may include one or more supercritical fluids (SCFs), inert gases such as noble gases, organic working fluids, or any combination thereof.
  • the SCF may include a supercritical carbon dioxide (sCCh) or sCCh blend having one or more dopants.
  • the noble gases may include helium (He), xenon (Xe), or a combination thereof (e.g., He- Xe mixture).
  • the inert gas may include nitrogen.
  • the organic working fluids may include hydrocarbons (HCs), fluorocarbons (PFCs). hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof.
  • the working fluid 916 may include the SCF, such as the sCCh or sCCh blend having one or more dopants.
  • the dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (CeFe), titanium tetrachloride (TiCh). or any combination of dopants.
  • the sCCh blend may have 5% to 20%mol dopants to increase the supercritical temperature of the sCCh.
  • the dopants may increase the critical temperature of the sCCh to about 70 to 100 degrees Celsius without a notable drop in efficiency.
  • the sCCh blend may increase the amount of waste heat quantity' by condensing the SCO2 blend at a higher temperature. As a result, all or substantially all of the waste heat rejected from the thermodynamic cycle 24 is available for use with the DAC system 18 as the thermal fluid 34.
  • the WHR system 22 may include any number of primary heat exchangers 914. such as 1, 2. 3, 4, 5, 6, 7. 8, 9, 10. or more primary heat exchangers 914.
  • the primary heat exchangers 914 include primary' heat exchangers 918 and 920.
  • the thermodynamic cycle 24 has a plurality of components 922 including, for example, one, two, or more compressors 924, waste heat recovery (WHR) heat exchangers 926, primary heat exchangers 914, recuperators 928 (e.g., heat exchangers), turbines 930, and pre-coolers 932 arranged along the fluid circuit 912, wherein the fluid circuit 912 includes a plurality' of fluid lines or conduits 934 between and fluidly connecting the components 922.
  • the components 922 also may include a plurality of valves and sensors disposed at, upstream from, and/or downstream from each of the components 922, wherein the controller 220 is communicatively coupled to the valves, the sensors, and the components 922 to control the thermodynamic cycle 24.
  • the one or more compressors 924 includes compressors 936 and 938.
  • the WHR heat exchangers 926 include a WHR heat exchanger 940
  • the recuperators 928 includes recuperators 942 and 944
  • the turbines 930 include turbines 946 and 948
  • the pre-coolers 932 include a pre-cooler 950.
  • the components 922 also include a flow mixer 952 and a flow splitter 954. The thermodynamic cycle 24 of FIG.
  • the primary heat exchangers 914 recover heat from the thermal fluid 30 to heat the working fluid 916, wherein the heat source 26 (e.g.. nuclear system 50, combustion system 52, and/or solar thermal system 54) provides heat for heating the thermal fluid 30.
  • the heat source 26 e.g.. nuclear system 50, combustion system 52, and/or solar thermal system 54
  • the WHR heat exchangers 926 rejects waste heat from the working fluid 916 as a heat source to provide the thermal fluid 34 from the thermodynamic cycle 24 to the gas capture systems 20 of the DAC system 18.
  • the components 922 of the thermodynamic cycle 24 are arranged along a relative high-pressure (HP) circuit portion 956 of the fluid circuit 912 downstream from the compressors 924 (e.g., compressor 936 and 938) and upstream from the turbines 930 (e.g., turbines 946 and 948), or a relatively low-pressure (LP) circuit portion 958 of the fluid circuit 912 downstream from the turbines 930 (e.g., turbines 946 and 948) and upstream from the compressors 924 (e.g., compressor 936 and 938).
  • HP relative high-pressure
  • LP relatively low-pressure
  • the compressors 924 transition from the LP circuit portion 958 to the HP circuit portion 956 of the fluid circuit 912 by compressing the working fluid 916.
  • the turbines 930 transition from the HP circuit portion 956 to the LP circuit portion 958 of the fluid circuit 912 by extracting work from the working fluid 916, thereby- reducing the pressure of the working fluid 916 and driving one or more loads 947 and 949 (e.g., mechanical loads and/or electrical generators) and shafts (e.g.. shafts coupled to the compressors 924).
  • loads 947 and 949 e.g., mechanical loads and/or electrical generators
  • shafts e.g. shafts coupled to the compressors 924.
  • the loads 947 and 949 are a primary- function of the thermodynamic cycle 24, such that the thermodynamic cycle 24 generates mechanical and/or electrical power using heat from the heat source 26.
  • the primary heat exchangers 918 and 920 are disposed along and fluidly couple to the fluid circuit 912 upstream from the respective turbines 946 and 948, such that the primary' heat exchanger 918 is along the HP circuit portion 956 and the primary- heat exchanger 920 is at a transition between the HP circuit portion 956 and the LP circuit portion 958 of the fluid circuit 912.
  • the recuperators 942 and 944 are disposed at respective intersections 960 and 962 between the HP circuit portion 956 and the LP circuit portion 958 of the fluid circuit 912.
  • the WHR heat exchangers 926 e.g., WHR heat exchanger 940
  • the pre-coolers 932 e.g., pre-cool er 950
  • the compressors 924 are configured to compress the working fluid 916 (e.g., working fluid 32) and supply the compressed working fluid 916 to the HP circuit portion 956.
  • the compressors 924 e.g., compressor 936 and 938) may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft, which is driven to rotate by the one or more turbines 930 (e.g., turbines 946 and 948) via one or more shafts.
  • the compressor 936 supplies the compressed working fluid 916 to the recuperator 942 at the intersection 960.
  • the recuperator 942 transfers heat between the working fluid 916 along the HP circuit portion 956 (e.g., between the compressor 936 and the flow mixer 952) and the LP circuit portion 958 (e.g., between the recuperator 944 and the flow splitter 954), thereby heating the working fluid 916 along the HP circuit portion 956 upstream from the flow mixer 952 and the turbines 930 and cooling the working fluid 916 along the LP circuit portion 958 upstream from the flow splitter 954 (and also the compressor 938 and the WHR heat exchanger 940).
  • the compressed working fluid 916 from the compressor 936 continues to flow through the HP circuit portion 956 to the flow mixer 952.
  • the compressor 938 supplies the compressed working fluid 916 to the flow mixer 952, such that the compressed working fluid 916 from both compressors 936 and 936 is mixed prior to delivery to the recuperator 944 at the intersection 962.
  • the recuperator 944 transfers heat between the working fluid 916 along the HP circuit portion 956 (e.g., between the flow mixer 952 and the primary heat exchanger 918) and the LP circuit portion 958 (e.g., between the turbine 948 and the recuperator 942).
  • the working fluid 916 continues to flow 7 along the HP circuit portion 958 from the recuperator 944 to the primary 7 heat exchanger 918.
  • the primary’ heat exchangers 914 are configured to use heat from the heat source 26 (e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54) to provide heat to the thermodynamic cycle 24 via the thermal fluid 30.
  • the primary' heat exchanger 918 transfers heat from the thermal fluid 30 along the flow path 910 (e.g., fluid circuit 110) to the working fluid 916 along the fluid circuit 912, thereby heating the working fluid 916 prior to the turbine 946.
  • the turbine 946 is driven by and expands the heated working fluid 916 from the primary 7 heat exchanger 918, and outputs a relatively lower pressure working fluid 916 to the next primary heat exchanger 920.
  • the primary heat exchanger 920 transfers heat from the thermal fluid 30 along the flow path 910 (e.g., fluid circuit 110) to the working fluid 916 along the fluid circuit 912, thereby heating the working fluid 916 prior to the turbine 948.
  • the turbine 948 is driven by and expands the heated w orking fluid 916 from the primary heat exchanger 920, and outputs a relatively lower pressure working fluid 916 for delivery along the LP circuit portion 958 to the recuperator 944 at the intersection 962 followed by the recuperator 942 at the intersection 960.
  • the thermodynamic cycle 24 may include any number of pairs (e.g., 1, 2, 3, 4, 5, or more) of primary' heat exchangers 914 and turbines 930, wherein each pair includes at least one of the primary heat exchangers 914 upstream from a corresponding one of the turbines 930.
  • the recuperators 942 and 944 transfer heat between the working fluid 916 along the HP circuit portion 956 and the LP circuit portion 958, thereby cooling the working fluid 916 prior to the flow splitter 954.
  • the flow splitter 954 directs a portion of the cooled working fluid 916 to the compressor 938, and a portion of the cooled working fluid 916 to the WHR heat exchangers 926 (e.g., WHR heat exchanger 940).
  • the WHR heat exchanger 940 is configured to transfer heat for cooling the working fluid 916 (e.g., cooled working fluid) along the LP circuit portion 958 between the flow splitter 954 and the pre-cooler 950. while heating the working fluid (e.g., thermal fluid 34) along the fluid circuit 130 coupled to the one or more gas capture systems 20 of the DAC system 18.
  • the WHR heat exchanger 940 may be configured to increase the temperature of the thermal fluid 34 to a temperature of approximately 100 to 150 degrees Celsius. 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, 130 to 150 degrees Celsius, or 110 to 130 degrees Celsius, or at least equal to or greater than approximately 100, 110, 120, 130, 140, or 150 degrees Celsius plus or minus 5 degrees Celsius.
  • the WHR heat exchanger 940 may be configured to decrease the temperature of the working fluid 916 to a temperature of approximately 50 degrees Celsius (e.g.. plus or minus 1. 2, 3, 4, or 5 degrees Celsius), or between approximately 40 to 60 degrees Celsius.
  • the pre-coolers 932 may include one or more heat exchangers configured to transfer heat away from the working fluid 916 to the environment (e.g., river water or ambient air), thereby reducing a temperature of the working fluid 916 upstream of the compressor 936.
  • the pre-coolers 932 e.g., pre-cooler 950
  • the pre-coolers 932 may be configured to decrease the temperature of the working fluid 916 to a temperature of approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or a temperature between 30 to 50 degrees Celsius, or between 40 to 50 degrees Celsius.
  • the working fluid 916 from the precooler 950 returns to the compressor 936 while the working fluid 916 from the flow splitter 954 returns to the compressor 938 for another pass through the fluid circuit 912 of the thermodynamic cycle 24.
  • the heat source 26 e.g., nuclear system 50, combustion system 52, and/or solar thermal system 54
  • the DAC system 18 uses waste heat extracted from the thermodynamic cycle 24 via the WHR heat exchangers 926 (e.g., WHR heat exchanger 940).
  • the WHR heat exchanger 940 is configured to extract or reject waste heat from the working fluid 916 to generate the thermal fluid 34. which is supplied to one or more gas capture systems 20 of the DAC system 18 via the fluid circuit 130.
  • the thermodynamic cycle 24 may reject the waste heat to the environment, such that the waste heat is not used for any useful purpose.
  • the thermal fluid 34 may transfer heat to the gas capture systems 20 during a desorption mode, thereby facilitating desorption of undesirable gases (e.g., CO2) from the air 190 or other gases. If the thermal fluid 34 contains excess heat beyond the needs of the DAC system 18, then the thermal storage system 140 stores the excess heat for later usage by the DAC system 18. For example, if the thermal fluid 34 contains insufficient heat to support the needs of the DAC system 18. then the thermal storage system 140 may provide the thermal fluid 34 to the DAC system 18.
  • undesirable gases e.g., CO2
  • FIGS. 1-6 may be used in any combination with one another.
  • the embodiments of FIGS. 1-6 are not intended to be mutually exclusive relative to one another.
  • the illustrated embodiments may be particularly well-suited for direct air capture to remove undesirable gases (e.g., CO2) from air, the illustrated embodiments may be used for gas capture from any gases.
  • thermodynamic cycles 24 and/or the thermal storage system 140 to provide thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18.
  • the thermodynamic cycles 24 may include one or more separate thermodynamic cycles. one or more loops or sections with heat exchangers and recuperators, or any suitable configuration based on FIGS. 1-6.
  • the thermodynamic cycles 24 are configured to provide heat to sorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof.
  • the heat source 26 that provides heat to the thermodynamic cycles 24 may include the nuclear system 50, the combustion system 52, and/or the solar thermal system 54. In some embodiments, only renewable energy sources or carbon-free energy sources may be used for the heat source 26. Accordingly, the nuclear system 50 and/or the solar thermal system 54 may help to provide a carbon negative power plant.
  • a system includes a direct air capture (DAC) system, including one or more gas capture systems configured to capture an undesirable gas from air.
  • the system further includes a thermodynamic cycle including a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid
  • the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid
  • the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • thermo storage system having one or more thermal storage media configured to store heat from the thermodynamic cycle and selectively provide the heat to the one or more gas capture systems.
  • thermochemical thermal energy storage examples include sensible thermal energy storage, latent thermal energy storage, and/or thermochemical thermal energy storage.
  • the one or more thermal storage media include one or more phase change materials.
  • the working fluid includes a supercritical fluid, an inert gas. a noble gas, an organic fluid, or any combination thereof.
  • the supercritical CO2 includes one or more dopants
  • the one or more dopants include sulfur dioxide (SO2), hexafluorobenzene (CeFe), titanium tetrachloride (TiCh), or any combination of dopants.
  • the working fluid includes one or more noble gases
  • the one or more noble gases include helium, xenon, or a combination thereof.
  • the one or more gas capture systems include a sorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or a combination thereof.
  • the heat source includes a solar thermal system having one or more solar collectors.
  • thermodynamic cycle includes a closed-loop Brayton cycle
  • heat source includes a nuclear system or a solar thermal system
  • undesirable gas includes carbon dioxide (CO2).
  • the one or more gas capture systems include a sorbent-based gas capture system
  • the working fluid includes a supercritical fluid, an inert gas, a noble gas, an organic fluid, or any combination thereof.
  • a system includes a controller having memory, a processor, and instructions stored on the memory' and executable by the processor to control a direct air capture (DAC) system including one or more gas capture systems to capture an undesirable gas from air.
  • the processor of the controller is further configured to control a thermodynamic cycle to provide heat to the one or more gas capture systems.
  • the thermodynamic cycle includes a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid
  • the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid
  • the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • thermodynamic cycle includes a closed-loop Brayton cycle
  • heat source includes a nuclear system or a solar thermal system
  • undesirable gas includes carbon dioxide (CO2)
  • the one or more gas capture systems include a sorbent-based gas capture system
  • the working fluid includes a supercritical fluid, an inert gas, a noble gas, an organic fluid, or any combination thereof.
  • a method includes controlling a direct air capture (DAC) system including one or more gas capture systems to capture an undesirable gas from air.
  • the method further includes controlling a thermodynamic cycle to provide heat to the one or more gas capture systems.
  • the thermodynamic cycle includes a fluid circuit having at least one compressor, at least one recuperator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger.
  • the fluid circuit is configured to circulate a working fluid, the at least one first heat exchanger is configured to transfer heat from a heat source to the working fluid, and the at least one second heat exchanger is configured to transfer heat from the working fluid to the one or more gas capture systems.
  • thermodynamic cycle includes a closed-loop Brayton cycle
  • heat source includes a nuclear system or a solar thermal system
  • undesirable gas includes carbon dioxide (CO2)
  • the one or more gas capture systems include a sorbent-based gas capture system
  • the working fluid includes a supercritical fluid, an inert gas, a noble gas, an organic fluid, or any combination thereof.

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Abstract

L'invention concerne un système qui comporte un système de capture directe d'air (CNA), comportant un ou plusieurs systèmes de capture de gaz conçus pour capturer un gaz indésirable dans l'air. Le système comporte en outre un cycle thermodynamique comportant un circuit de fluide présentant au moins un compresseur, au moins un récupérateur, au moins une turbine, au moins un premier échangeur de chaleur et au moins un second échangeur de chaleur. Le circuit de fluide est conçu pour faire circuler un fluide de travail, le ou les échangeurs de chaleur sont conçus pour transférer de la chaleur d'une source de chaleur au fluide de travail, et le ou les seconds échangeurs de chaleur sont conçus pour transférer de la chaleur du fluide de travail à un ou plusieurs systèmes de capture de gaz.
PCT/US2024/026883 2024-04-29 2024-04-29 Système et procédé de capture directe d'air à l'aide de chaleur perdue Pending WO2025230511A1 (fr)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4414813A (en) * 1981-06-24 1983-11-15 Knapp Hans J Power generator system
US20150069758A1 (en) * 2013-05-31 2015-03-12 Chal S. Davidson Systems and methods for power peaking with energy storage
US20200270496A1 (en) * 2017-09-12 2020-08-27 Politecnico Di Milano Co2-based mixtures as working fluid in thermodynamic cycles
US20230375277A1 (en) * 2022-05-20 2023-11-23 University Of North Texas Process and system for heat exchange process
US20230417494A1 (en) * 2022-06-24 2023-12-28 Baltimore Aircoil Company, Inc. Heat transfer apparatus and method
US20240009613A1 (en) * 2020-08-17 2024-01-11 Susteon Inc. Co2 capture sorbents with low regeneration temperature and high desorption rates

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4414813A (en) * 1981-06-24 1983-11-15 Knapp Hans J Power generator system
US20150069758A1 (en) * 2013-05-31 2015-03-12 Chal S. Davidson Systems and methods for power peaking with energy storage
US20200270496A1 (en) * 2017-09-12 2020-08-27 Politecnico Di Milano Co2-based mixtures as working fluid in thermodynamic cycles
US20240009613A1 (en) * 2020-08-17 2024-01-11 Susteon Inc. Co2 capture sorbents with low regeneration temperature and high desorption rates
US20230375277A1 (en) * 2022-05-20 2023-11-23 University Of North Texas Process and system for heat exchange process
US20230417494A1 (en) * 2022-06-24 2023-12-28 Baltimore Aircoil Company, Inc. Heat transfer apparatus and method

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