System and method for direct air capture using waste heat

Abstract

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 also 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, 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.

Description

Background Technology

[0001] This application relates in its entirety to a system and method for capturing unwanted gases from air or other gases.

[0002] The atmosphere contains air and various undesirable gases. For example, undesirable gases may include carbon oxides (CO). X Such as carbon dioxide (CO2) and carbon monoxide (CO), nitrogen oxides (NO) X Such as nitrogen dioxide (NO2) and / or sulfur oxides (SO4). X Examples include sulfur dioxide (SO2). CO2 is both an acid gas and a greenhouse gas. Unfortunately, atmospheric CO2 levels have generally increased over thousands of years and currently exceed approximately 420 parts per million (ppmv) by volume or 643 parts per million (ppmw) by weight. With the emergence of various regulations and environmental concerns regarding global warming, there is a desire to reduce undesirable gases in the atmosphere, such as CO2. Summary of the Invention

[0003] The following outlines some embodiments that are comparable to the scope of the originally claimed subject matter. These embodiments are not intended to limit the scope of the claimed embodiments, but rather are intended only to provide a brief overview of the possible forms of the subject matter. In practice, the currently claimed embodiments may include a variety of forms that may be similar to or different from those set forth below.

[0004] In some embodiments, a system includes a direct air capture (DAC) system comprising one or more gas capture systems configured to capture unwanted gases from the air. The system also includes a thermodynamic cycle comprising a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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.

[0005] In some embodiments, a system includes a controller having a memory, a processor, and instructions stored in the memory and executable by the processor to control a direct air capture (DAC) system comprising one or more gas capture systems to capture unwanted gases from the air. The controller's processor is also configured to control a thermodynamic cycle to provide heat to the one or more gas capture systems. The thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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.

[0006] In some embodiments, a method includes controlling a direct air capture (DAC) system comprising one or more gas capture systems to capture unwanted gases from the air. The method also includes controlling a thermodynamic cycle to provide heat to the one or more gas capture systems. The thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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. Attached Figure Description

[0007] These and other features, aspects, and advantages of the currently disclosed technology will be better understood when the following detailed description is read with reference to the accompanying drawings, in which the same characters denote the same parts, wherein:

[0008] Figure 1 This is a block diagram of an implementation scheme for a combined cycle system, which includes a heat source, a steam generation system, a steam turbine system, a direct air capture (DAC) system with one or more gas capture systems, and a waste heat recovery system with a thermodynamic cycle and a heat storage system configured to provide heat fluid to the gas capture system.

[0009] Figure 2 yes Figure 1 A schematic diagram of an implementation scheme for a gas capture system illustrates an adsorbent-based gas capture system with adsorption, desorption, and cooling modes, wherein a waste heat recovery system provides heat fluid for the desorption mode.

[0010] Figure 3 yes Figure 1A schematic diagram of an implementation scheme for a gas capture system illustrates a solvent-based gas capture system with an absorber and a stripper, wherein a waste heat recovery system provides a hot fluid to the stripper.

[0011] Figure 4 yes Figure 1 The schematic diagram illustrates the implementation scheme of the combined cycle system, which is an example of the implementation scheme of the thermodynamic cycle of the waste heat recovery system.

[0012] Figure 5 yes Figure 1 The schematic diagram illustrates the implementation scheme of the combined cycle system, which is an example of the implementation scheme of the thermodynamic cycle of the waste heat recovery system.

[0013] Figure 6 yes Figure 1 The schematic diagram illustrates the implementation scheme of the combined cycle system, which is an example of the implementation scheme of the thermodynamic cycle of the waste heat recovery system. Detailed Implementation

[0014] The following describes one or more specific implementations of the systems and methods disclosed herein. To provide a concise description of these implementations, not all characteristics of an actual implementation may be described in the specification. It should be understood that, as in any engineering or design project, the development of any such actual implementation requires numerous implementation-specific decisions to achieve the developer's specific objectives, such as complying with system-related and business-related constraints, which may vary from implementation to implementation. Furthermore, it should be understood that such development work may be complex and time-consuming, but remains a routine task of design, fabrication, and manufacturing for those skilled in the art who benefit from this disclosure.

[0015] When describing elements of various embodiments in the currently disclosed implementation schemes, the articles “a,” “an,” “the,” and “the” are intended to mean that one or more of the elements are present. The terms “comprising,” “including,” and “having” are intended to be inclusive and mean that additional elements may be present in addition to those listed.

[0016] The disclosed embodiments include systems and methods for reducing unwanted gases in the atmosphere using a direct air capture (DAC) system having one or more gas capture systems. The gas capture system is configured to remove unwanted gases (e.g., CO2) from air or any other gas. The gas capture system may include adsorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or combinations thereof. In some embodiments, the gas capture system (e.g., an adsorbent-based gas capture system) may include one or more temperature-switching adsorption (TSA) systems, vacuum temperature-switching adsorption (VTSA) systems, variable concentration adsorption (CSA) systems, or any combination thereof. For example, a gas capture system (e.g., an adsorbent-based gas capture system) may include one or more temperature-switching adsorption (TSA) units or adsorbers that rely on temperature fluctuations to adsorb unwanted gases at a first temperature (e.g., a low temperature) and desorb unwanted gases at a second temperature (e.g., a high temperature). For example, a gas capture system (e.g., an adsorbent-based gas capture system) may include one or more temperature-variable adsorption (VTSA) units or adsorbers that rely on temperature and pressure fluctuations to adsorb unwanted gases at a first temperature (e.g., low temperature) and a first pressure (e.g., high pressure) and desorb unwanted gases at a second temperature (e.g., high temperature) and a second pressure (e.g., low pressure).

[0017] In some embodiments, the heat source facilitating desorption during desorption may include a variety of heated fluids, such as steam, inert gases (e.g., nitrogen (N2)), or any other suitable purge gas. As discussed in detail below, one or more thermodynamic cycles configured to receive heat from one or more heat sources (e.g., nuclear reactors, combustion systems, and / or solar thermal systems) and generate electricity may also be configured with a waste heat recovery (WHR) system to provide heat that would otherwise be wasted to the gas capture process, thereby helping to reduce the overall operating cost of the gas capture process. For example, the system may include a thermodynamic cycle (e.g., a Brayton cycle) configured to provide waste heat to the gas capture system via a WHR. As discussed further in detail below, the thermodynamic cycle may use one or more of the following working fluids: supercritical fluids, inert gases (such as rare gases), organic working fluids, or any combination thereof. Using waste heat to support the gas capture process helps reduce the overall cost of gas capture, thereby helping to facilitate the commercialization of gas capture systems.

[0018] Adsorbent-based gas capture systems are configured to adsorb unwanted gases into an adsorbent material, followed by desorption of the unwanted gases from the adsorbent material using a heat source (e.g., a heated fluid). The adsorption process is exothermic, while the desorption process is endothermic. As discussed in detail below, the thermodynamic cycle of the WHR system is coupled as a heat source to the adsorbent-based gas capture system (e.g., a desorption mode, stage, or section) to provide heat (e.g., a heated fluid) to facilitate the desorption process. Therefore, the thermodynamic cycle of the WHR system can significantly reduce or eliminate the need for additional heat sources to support the desorption process.

[0019] Solvent-based gas capture systems may include: an absorber configured to absorb unwanted gases into a solvent; and a stripper configured to strip unwanted gases from the solvent using a heat source (e.g., a heated fluid). Although solvent-based gas capture systems are discussed as using a solvent as the absorbent fluid, the disclosed embodiments may use any suitable absorbent fluid to capture unwanted gases. Therefore, solvent-based gas capture systems may also be described as fluid-based absorbent gas capture systems. As discussed in detail below, the thermodynamic cycle of the WHR system is coupled to the solvent-based gas capture system (e.g., the stripper) as a heat source, thereby providing heat (e.g., a heated fluid) to facilitate the desorption process. Thus, the thermodynamic cycle of the WHR system can significantly reduce or eliminate the need for additional heat sources to support the desorption process.

[0020] As discussed below, the thermodynamic cycle of a WHR system can be used in conjunction with a gas capture system in a variety of configurations. Although specific examples are provided below, the thermodynamic cycle of a WHR system can be used in any suitable manner to support a wide range of gas capture systems, including but not limited to adsorbent-based gas capture systems, solvent-based gas capture systems, and cryogenic gas capture systems.

[0021] Figure 1This is a block diagram of an embodiment of a combined cycle system 10, which includes a power generation system 12, a steam turbine system 14, a steam generation system 16, a direct air capture (DAC) system 18 with 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., a Brayton cycle). The power generation system 12 includes a heat source 26 with multiple thermoelectric power generation systems 28 configured to provide heat to drive the steam generation system 16 and the thermodynamic cycle 24. For example, the steam generation system 16 uses heat to generate steam to supply power to one or more steam turbine systems 14, which in turn drive one or more loads 100 (e.g., mechanical loads and / or generators). By another example, heat drives the operation of the thermodynamic cycle 24, which in turn drives one or more loads 25 (e.g., mechanical loads and / or generators). Thus, the power generation system 12, the steam turbine system 14, the steam generation system 16, and the thermodynamic cycle 24 can operate together to generate electricity, such as for use in a power grid. In addition to its primary function of generating electricity, thermodynamic cycle 24 can provide waste heat to one or more gas capture systems 20 of DAC system 18 via WHR system 22. Otherwise, the waste heat of thermodynamic cycle 24 would not be used by thermodynamic cycle 24 and would be released into the environment. Therefore, WHR system 22 uses the waste heat of thermodynamic cycle 22 as a heat source for DAC system 18, thereby helping to reduce the costs associated with operating DAC system 18.

[0022] One or more gas capture systems 20 of DAC system 18 are configured to capture unwanted gases (e.g., CO2) from gases such as air. Gas capture systems 20 may include adsorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof. WHR system 22 uses heat from power generation system 12 (e.g., waste heat such as heat fluid 30) to heat working fluid 32 of thermodynamic cycle 24, which in turn provides heat (e.g., waste heat such as heat fluid 34) to operate one or more gas capture systems 20 of DAC system 18. For example, thermodynamic cycle 24 may include one or more heat exchangers (e.g., regenerators or coolers) configured to transfer heat from heat fluid 30 to working fluid 32 and one or more heat exchangers configured to transfer heat from working fluid 32 to heat fluid 34. In some embodiments, thermodynamic cycle 24 (e.g., Brayton cycle) is a thermodynamic power cycle or a thermodynamic heat pump cycle. Thermodynamic cycle 24 may also be described as a thermodynamic cycle system (e.g., a Brayton cycle system), such as a thermodynamic power cycle system or a thermodynamic heat pump cycle system. Additionally, in some embodiments, the working fluid 32 includes one or more of a supercritical fluid (SCF), an inert gas (such as a rare gas), an organic working fluid, or any combination thereof. Additionally, in some embodiments, the working fluid 32 does not include combustion gases (e.g., exhaust gas, flue gas), and the thermodynamic cycle 24 does not include a combustion system that provides combustion gases as the working fluid 32. Instead, the thermodynamic cycle 24 relies on waste heat from the heat source 26. The heat fluid 34 may be configured to transfer heat to one or more gas capture systems 20 to achieve or improve the desorption of undesirable gases (e.g., CO2) during desorption mode.

[0023] Before discussing the details of the DAC system 18, various aspects of the combined circulation system 10 will be discussed in further detail. For the purposes of orientation in the figures, reference may be made to the axial direction or axis 40, the radial direction or axis 42 extending radially away from the axial direction or axis 40, and the circumferential direction or axis 44 extending circumferentially around the axial direction or axis 40. For example, directions or axes 40, 42, and 44 may be referenced to the axis of rotation of the steam turbine system 14.

[0024] As noted above, the power generation system 12 includes a heat source 26 having multiple thermal power generation systems 28 configured to supply heat to the steam generation system 16. In an illustrated embodiment, the thermal power generation system 28 includes a nuclear system 50 (e.g., a nuclear reactor system), a combustion system 52, and a solar thermal system 54. Additionally, 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 a nuclear fusion reaction, thereby supplying heat to the steam generator 56 to generate steam 62. The combustion system 52 may include a furnace or combustion vessel configured to burn fuel (e.g., coal, biofuel, liquid fuel, gaseous fuel, etc.) to generate hot combustion gases, which in turn supply heat to the steam generator 58 to generate steam 64. The solar thermal system 54 may include multiple solar collectors configured to utilize solar energy to supply heat to the steam generator 60 to generate steam 66. The steam 62, 64, and 66 provided by the respective steam generators 56, 58, and 60 may include one or more steam streams of high-pressure steam (HP steam), medium-pressure steam (IP steam), low-pressure steam (LP steam), or combinations thereof. In some embodiments, the power generation system 12 may include and / or exclude any one of the plurality of thermal power generation systems 28, and thus the nuclear system 50, combustion system 52, and solar thermal system 54 may be used individually or in any combination thereof. In some embodiments, the combustion system 52 may or may not include a gas turbine system having a compressor section, a combustor section, and a turbine section driven by the hot combustion gases generated in the combustor section.

[0025] Steam turbine system 14 may receive one or more steam flows of steam 62, 64, and / or 66 via steam circuits 68, 70, and 72, which include corresponding valves 74, 76, and 78. 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. Steam turbine system 14 may direct 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. In the illustrated embodiment, steam turbine system 14 delivers steam 62, 64, and / or 66 through HP steam turbine 80 to drive turbine blades, and then steam circuit 86 delivers intermediate-pressure steam to IP steam turbine 82. Intermediate-pressure steam flows through IP steam turbine 82 to drive turbine blades, and then steam circuit 88 delivers low-pressure steam to LP steam turbine 84. Low-pressure steam flows through LP steam turbine 84 to drive the turbine blades, and then condensate circuit 90 delivers the output from LP steam turbine 84 back to steam generation system 16 (e.g., steam generators 56, 58, and / or 60). As shown, condensate circuit 90 includes condenser 92 configured to condense any remaining steam into condensate (e.g., condensate water), and pump 94 configured to pump the condensate back to steam generation system 16. Condensate circuit 90 also includes valve 96 configured to control the flow of condensate. In operation, steam turbines 80, 82, and 84 may be coupled to the same or different shafts 98, which are coupled to one or more loads 100, such as generators. The generator is configured to generate electricity for local use or for distribution on the power grid.

[0026] Therefore, power generation system 12 can be described as an electric power generation system. Nuclear system 50, steam generator 56, steam turbine system 14, and load 100 (e.g., generator) can be defined as a nuclear-driven power generation system 102. Combustion system 52, steam generator 58, steam turbine system 14, and load 100 (e.g., generator) can be defined as a combustion-driven power generation system 104. Solar thermal system 54, steam generator 60, steam turbine system 14, and load 100 (e.g., generator) can be defined as a solar-driven power generation system 106. In some embodiments, power generation system 12 may exclude combustion system 52 while including one or more of nuclear system 50 and / or solar thermal system 54 to define a carbon-free power generation system.

[0027] The power generation system 12 serves as a heat source 26 (e.g., via one or more of a plurality of thermal power generation systems 28 and steam generation systems 16) to supply hot fluid 30 to the thermodynamic cycle 24 of the WHR system 22. In an illustrated embodiment, the thermodynamic cycle 24 is coupled to the power generation system 12 via one or more fluid loops 110, which include a supply loop 112 and a return loop 114. The one or more fluid loops 110 may include one or more valves, such as valves 116 and 118, respectively coupled to the supply loop 112 and the return loop 114. Valves 116 and 118 are configured to control the supply and return flow of hot fluid 30 between the power generation system 12 and the thermodynamic cycle 24. In some embodiments, the one or more fluid loops 110 include fluid loops coupled to or through the nuclear system 50 and / or the steam generator 56, fluid loops coupled to or through the combustion system 52 and / or the steam generator 58, and fluid loops coupled to or through the solar thermal system 54 and / or the steam generator 60. The heat fluid 30 may include heated water and / or steam from steam generators 56, 58 and / or 60, nuclear system 50, combustion system 52, solar thermal system 54, or any combination thereof. In some embodiments, the heat fluid 30 may or may not include hot combustion gases or flue gas from combustion system 52.

[0028] Thermodynamic cycle 24 of WHR system 22 is configured to transfer heat away from hot fluid 30 (e.g., hot or heated hot fluid) received via supply circuit 112 of fluid circuit 110, transfer heat to working fluid 32 circulating in thermodynamic cycle 24, generate electricity or work in conjunction with thermodynamic cycle 24, and return hot fluid 30 (e.g., cold or cooled hot fluid) to power generation system 12 via return circuit 114 of fluid circuit 110. Thermodynamic cycle 24 may include Brayton cycles, such as closed-loop Brayton cycles. In some embodiments, 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.

[0029] As noted above, the working fluid 32 may include one or more supercritical fluids (SCFs), inert gases (such as rare gases), organic working fluids, or any combination thereof. For example, the SCF may include supercritical carbon dioxide (sCO2) or a blend of sCO2 with one or more dopants. Dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants. In some embodiments, the sCO2 blend may have 5% mol to 20% mol of dopants to increase the supercritical temperature of sCO2. For example, the dopants may increase the critical temperature of sCO2 to about 70°C to 100°C without a significant decrease in efficiency. Therefore, the amount of waste heat can be increased by condensing the sCO2 blend at a higher temperature. Thus, all or substantially all of the waste heat discharged from the thermodynamic cycle 24 can be used as heat fluid 34 for the DAC system 18. In some embodiments using SCF as the working fluid 32, the thermodynamic cycle 24 may be described as an SCF-based cycle or an SCF cycle. By further example, the rare gas may include helium (He), xenon (Xe), or combinations thereof (e.g., a He-Xe mixture). By further example, the inert gas may include nitrogen. By further example, the organic working fluid may include hydrocarbons (HCs), perfluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof.

[0030] Regardless of the specific working fluid 32, the thermodynamic cycle 24 of the WHR system 22 is configured to use waste heat to support the DAC system 18. In an illustrated embodiment, the WHR system 22 includes one or more fluid loops 130 extending between the thermodynamic cycle 24 and the DAC system 18 (e.g., the gas capture system 20). For example, the fluid loop 130 may include one or more supply loops 132 and one or more return loops 134. The fluid loop 130 also includes one or more valves, such as valves 136 and 138 respectively disposed along the supply loop 132 and the return loop 134. Valves 136 and 138 are configured to control the supply and return flow of the hot fluid 34 between the thermodynamic cycle 24 and the gas capture system 20 of the DAC system 18. In operation, the 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 to the hot fluid 34 (e.g., hot or heated hot fluid) supplied via the supply loop 132. Subsequently, the gas capture system 20 of the DAC system 18 is configured to transfer heat away from the hot fluid 34 (e.g., hot or heated hot fluid) received via the supply loop 132, use the heat as needed to support the desorption mode or process, and then return the hot fluid 34 (e.g., cold or cooled hot fluid) to the thermodynamic cycle 24 via the return loop 134.

[0031] In some embodiments, the heat fluid 34 may contain heat (e.g., waste heat) exceeding the heat requirements of the gas capture system 20 of the DAC system 18. Therefore, in some embodiments, the WHR system 22 also includes a heat storage system 140 having one or more heat storage units or media 142, 144, 146, and 148. Each of the heat 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. For example, latent thermal energy storage may include phase change materials (PCMs). PCMs may include solid-liquid PCMs, solid-solid PCMs, solid-gas PCMs, liquid-gas PCMs, or any combination thereof. Typically, PCMs are configured to absorb heat during a phase change and subsequently release heat when needed to support the DAC system 18. For example, for a solid-liquid PCM, the phase change may be between a solid and a liquid phase, or for a solid-solid PCM, the phase change may be between different solids (e.g., different crystalline structures). In some embodiments, the PCM may include any suitable transition between or between a solid, liquid, and gaseous phase. The PCM may be stored or contained in one or more enclosures, such as the internal chambers of a thermally insulated enclosure, multiple microencapsulations (e.g., microcapsules), or combinations thereof. As an example, solid-solid PCMs may change their crystalline structure from one lattice configuration to another within an operating temperature range of 50°C to 175°C. As another example, polyurethane PCMs may have an operating temperature range of 20°C to 36°C. For other solid-solid PCMs, such as polymer PCMs, and various solid-liquid PCMs, such as paraffin wax, inorganic hydrates (Na₂SO₄·10H₂O), bio-PCMs (e.g., organic fatty acid ester PCMs made from natural resources such as soybean and palm oil), and sodium acetate trihydrate (SAT, C₂H₹NaO₅), the operating temperature range may vary.

[0032] In some embodiments, when excess waste heat is available, the WHR system 22 selectively enables heat transfer from fluid circuit 130 to heat storage system 140 via fluid circuit 150. As shown, fluid circuit 150 includes a supply circuit 152 and a return circuit 154 extending between heat storage system 140 and supply circuit 132. Fluid circuit 150 also includes one or more valves, such as valves 156 and 158 along supply circuit 152 and return circuit 154, respectively. Valves 156 and 158 are configured to open, close, and generally regulate the supply and return flow of hot fluid 34 between supply circuit 132 and heat storage system 140. When valves 156 and 158 are open, hot fluid 34 transfers heat to heat storage units or media 142, 144, 146, and 148 in heat storage system 140. If the heat storage units or media 142, 144, 146, and 148 are fully thermally loaded and excess waste heat is still available, the WHR system 22 may selectively direct the hot fluid 34 to another system to utilize the waste heat, and / or the WHR system 22 may enable the waste heat discharge system 160 to discharge the waste heat into the atmosphere. For example, the waste heat discharge system 160 may include a heat exchanger 162 coupled to the heat storage system 140 via a fluid loop 164, wherein the fluid loop 164 circulates the hot fluid 34 and / or coolant fluid through the heat exchanger 162 to discharge the waste heat into the atmosphere, as indicated by arrow 166. In some embodiments, if the hot fluid 34 is unavailable and / or cannot meet the thermal requirements of the gas capture system 20 of the DAC system 18, the heat storage system 140 is configured to provide stored heat (e.g., as the hot fluid 34) to the gas capture system 20.

[0033] As noted above, the DAC system 18 includes one or more gas capture systems 20 configured to capture unwanted gases from air 190 and / or one or more other gases, and output a treated gas (e.g., treated air 191) substantially free of unwanted gases. For example, the gas capture systems 20 may include any or any combination of gas capture systems 192 and 194, each having multiple components (e.g., components 196, 198, 200, and 202). The gas capture systems 20 (e.g., 192 and 194) are configured to obtain captured gas 204 from air 190. In an illustrated embodiment, the gas capture systems 20 (e.g., 192 and 194) may capture carbon dioxide (CO2) and output it as captured gas 204, which may be further directed to a compression system 206. For example, 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 a storage device and / or conduit 208. In some embodiments, air 190 is compressed by one or more compressors 210 along an intake circuit 212 coupled to the DAC system 18. In some embodiments, captured gas 204 may be supplied to the system to produce new products, such as an input stream for liquefied carbon-based fuels.

[0034] Gas capture systems 20 (e.g., 192 and 194) may include adsorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or any combination thereof configured to remove and capture unwanted gases from air 190 and / or other gases. In some embodiments, gas capture systems 20 (e.g., 192 and 194) may be configured to remove and capture unwanted gases, such as carbon oxides (CO). X (e.g., carbon dioxide (CO2) and carbon monoxide (CO)), and therefore gas capture system 20 can be described as a carbon capture system. In some embodiments, gas capture system 20 (e.g., 192 and 194) can be configured to remove and capture undesirable gases, such as nitrogen oxides (NOx). X (e.g., nitrogen dioxide (NO2)), and therefore the gas capture system 20 can be described as NO X Gas capture system. In some embodiments, gas capture systems 20 (e.g., 192 and 194) may be configured to remove and capture undesirable gases, such as sulfur oxides (SO₄). X (e.g., sulfur dioxide (SO2)), and therefore the gas capture system 20 can be described as SO XCapture System. In the following discussion, gas capture systems 20 (e.g., 192 and 194) may be described as adsorbent-based carbon capture systems, for example, using adsorbent materials and / or solvent-based carbon capture systems, for example, using liquid absorbents (e.g., solvents). However, the embodiments disclosed herein may use gas capture systems 20 (e.g., 192 and 194) of any type or configuration as indicated above.

[0035] Each gas capture system in gas capture systems 20 (e.g., 192 and 194) may include components 196, 198, 200, and 202. For adsorbent-based gas capture systems 20 (e.g., 192 and 194), components 196, 198, 200, and 202 may include adsorbent material disposed on or in a conduit (e.g., adsorption conduit, desorption conduit, and cooling conduit), contactor, cylinder, moving bed, rotating wheel, or any combination thereof along a flow path of air 190. The adsorbent-based gas capture system 20 is configured to adsorb unwanted gases (e.g., CO2) into the adsorbent material in adsorption mode and desorb unwanted gases from the adsorbent material in desorption mode. Components 196, 198, 200, and 202 may include a cooling system for helping to control the temperature of the adsorbent material (e.g., maintaining the adsorbent temperature within an upper and lower temperature threshold range) to improve the efficiency of the adsorption mode. The cooling system may include heat exchangers (e.g., finned and tubular heat exchangers), heat pipes, and other thermal control systems coupled to the adsorbent material to help control its temperature. Components 196, 198, 200, and 202 may also include heating systems, such as heated fluid systems (e.g., steam systems, electric heaters, waste heat systems, etc.), configured to apply heat to the adsorbent material during desorption mode to desorb unwanted gases from it. For example, the thermodynamic cycle 24 and / or thermal storage system 140 of the WHR system 22 are configured to provide a heated fluid 34 to the adsorbent material during desorption mode. Components 196, 198, 200, and 202 may also 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 adsorbent material during cooling mode. The adsorbent-based gas capture system 20 may also include other suitable components 196, 198, 200, and 202 to support the adsorbent material.

[0036] For the solvent-based gas capture system 20 (e.g., 192 and 194), components 196, 198, 200, and 202 may include one or more absorbers, one or more strippers, and a solvent loop through the absorbers and strippers. The absorber is configured to absorb an undesired gas (e.g., CO2) into the solvent in an absorption mode, thereby outputting a treated gas (e.g., treated air or other gas) and a gas-rich solvent (e.g., a CO2-rich solvent). The stripper is configured to strip the undesired gas from the gas-rich solvent in a desorption mode, thereby outputting a gas-lean solvent (e.g., a CO2-lean solvent) back to the absorber and outputting captured gas 204. Components 196, 198, 200, and 202 may include a cooling system coupled to the absorber, wherein the cooling system is configured to extract the heat generated by the absorption mode to help control the solvent temperature (e.g., maintain the solvent temperature within an upper and lower temperature threshold range) to improve the efficiency of the absorption mode. The cooling system may include heat exchangers (e.g., finned and tubular heat exchangers), heat pipes, and other thermal control systems coupled to the absorber to help control the solvent temperature. Components 196, 198, 200, and 202 may also include heating systems coupled to the stripper, such as heated fluid systems (e.g., steam systems, electric heaters, waste heat systems, etc.), wherein the heating systems are configured to apply heat to the rich-gas solvent during desorption mode to desorb unwanted gases from the rich-gas solvent. For example, the thermodynamic cycle 24 and / or thermal storage system 140 of the WHR system 22 are configured to provide a hot fluid 34 to the rich-gas solvent during desorption mode. Components 196, 198, 200, and 202 may also include a reboiler coupled to the stripper, pumps and valves for controlling the flow rate of solvent through the solvent loop between the absorber and the stripper, and heat exchangers for cooling the lean-gas solvent supplied to the absorber and heating the rich-gas solvent supplied to the stripper. The solvent-based gas capture system 20 may also include other suitable components 196, 198, 200, and 202 to support the absorber and stripper.

[0037] In the illustrated embodiment, the combined cycle system 10 also includes a controller 220 connected to the power generation 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 heat storage system 140, and various sensors 222 distributed throughout the combined cycle system 10. In the illustrated embodiment, the controller 220 includes one or more processors 224, a memory 226, instructions 228 stored in the memory 226 and executable by the processors 224, and communication circuitry 230 configured to communicate with the sensors 222 and various equipment throughout the combined cycle system 10. For example, the controller 220 is configured to control the nuclear system 50, the combustion system 52, and / or the solar thermal system 54 to provide heat to the respective steam generators 56, 58, and 60, thereby providing steam 62, 64, and 66 to operate the steam turbine system 14. Controller 220 may also control valves 74, 76, 78, and 96, as well as pump 94, to facilitate the flow between controllable steam generators 56, 58, and 60 and steam turbine system 14. By another example, controller 220 is configured to control valves 116 and 118 to control the flow of hot fluid 30 between power generation system 12 and thermodynamic cycle 24, thereby facilitating control of heat transfer to thermodynamic cycle 24. By another example, controller 220 is configured to control valves 136 and 138 to control the flow of hot fluid 34 between thermodynamic cycle 24 and DAC system 18, thereby facilitating control of heat transfer to one or more gas capture systems 20 (e.g., 192 and 194). By another example, controller 220 is configured to control valves 156 and 158 to control the flow of hot fluid 34 between heat storage system 140 and fluid loop 130, thereby facilitating control of excess heat storage and the release of stored heat for use in one or more gas capture systems 20 (e.g., 192 and 194). In some embodiments, controller 220 is configured to control the operation of gas capture system 20 (e.g., 192 and 194), such as by controlling operating modes (e.g., adsorption mode, desorption mode, cooling mode), controlling WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140) to control the flow rate and temperature of the thermal fluid 34 supplied to gas capture system 20, controlling the flow rate of various fluids through gas capture system 20, or any combination thereof.

[0038] Sensor 222 (labeled "S") is configured to monitor various operating parameters of the combined circulation system 10. In some embodiments, sensor 222 includes a temperature sensor, a pressure sensor, a flow rate sensor, a fluid composition sensor (e.g., a gas composition sensor), or any combination thereof. Sensor 222 may monitor parameters (e.g., temperature, pressure, flow rate, and fluid composition) at one or more locations of the DAC system 18, WHR system 22, thermodynamic cycle 24 (e.g., working fluid 32), thermal storage system 140, hot fluid 30, hot fluid 34, steam 62, 64 and / or 66, steam generators 56, 58 and 60, steam turbine system 14, nuclear system 50, combustion system 52, solar thermal system 54, or any combination thereof. By further example, sensor 222 may monitor the temperature of the hot fluid 34 supplied to the gas capture system 20, the temperature of the adsorbent material in an adsorbent-based gas capture system, the temperature of the solvent in a solvent-based gas capture system, or any combination thereof. In response to feedback from sensor 222, controller 220 may adjust the operating mode, fluid flow rate, heating, cooling, or any combination thereof in gas capture system 20. Additionally, in response to feedback from sensor 222, controller 220 may adjust the operating mode, fluid flow rate, heat transfer, compressor compression, turbine expansion, or any combination thereof in thermodynamic cycle 24.

[0039] As discussed below, a portion of the heat not used to generate electricity in thermodynamic cycle 24 (such as excess heat or waste heat) is used to generate heat fluid 34 to support one or more gas capture systems 20 of DAC system 18. Heat fluid 34 may include heated gas or liquid, such as heated water and / or steam. In some embodiments, heat fluid 34 may be the same fluid as or a different fluid from the working fluid 32 in thermodynamic cycle 24. Additionally, in some embodiments, heat fluid 34 may be the same fluid as or a different fluid from the fluid used in gas capture system 20. At one or more locations in thermodynamic cycle 24, heat exchangers (e.g., regenerators) may transfer heat from working fluid 32 (e.g., waste heat discharge) to heat fluid 34 at temperatures suitable for achieving desorption of undesired gases (e.g., CO2) in one or more gas capture systems 20. The temperature of the working fluid 32 at one or more locations in the thermodynamic cycle 24 can be 100 to 150 degrees Celsius, 110 to 150 degrees Celsius, 120 to 150 degrees Celsius, or 130 to 150 degrees Celsius. For example, waste heat discharge from the working fluid 32 to the hot fluid 34 can occur at a temperature at least equal to or greater than 100, 110, 120, 130, 140, or 150 degrees Celsius. Therefore, the hot fluid 34 can provide heat in one or more gas capture systems 20 to enable desorption within 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. For example, the hot fluid 34 can be provided to the gas capture system 20 to support desorption at a temperature of at least equal to or greater than 100 degrees Celsius, 110 degrees Celsius, 120 degrees Celsius, 130 degrees Celsius, 140 degrees Celsius, or 150 degrees Celsius plus or minus 5 degrees Celsius.

[0040] Figure 2 yes Figure 1A schematic diagram of an embodiment of the gas capture system 20 of the DAC system 18 illustrates an adsorbent-based gas capture system 250. In the illustrated embodiment, the adsorbent-based gas capture system 250 includes multiple adsorbent-based gas capture components or units 252 (e.g., adsorbers or adsorption units) associated with multiple corresponding conduits 254 such as conduits 256, 258, and 260 (e.g., adsorbent-containing conduits). The adsorbent-based gas capture unit 252 may include a temperature-switching adsorption (TSA) unit or adsorber, wherein temperature fluctuations or variations are used to alternate between an adsorption mode at a first temperature and a desorption mode at a second temperature. The first temperature is lower than the second temperature. The lower first temperature enables the adsorbent-based gas capture unit 252 to adsorb unwanted gases, wherein the lower temperature generally increases the capacity for adsorbing unwanted gases. The higher second temperature enables the adsorbent-based gas capture unit 252 to desorb unwanted gases, which can then be captured and used for other downstream processes.

[0041] In the illustrated embodiment, the adsorbent-based gas capture unit 252 includes adsorbent-based gas capture units 252A, 252B, and 252C associated with conduits 256, 258, and 260. Conduits 254 (e.g., 256, 258, and 260) may be lined with adsorbent along their inner surfaces, filled with adsorbent within their internal volumes, or typically filled with at least 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, or more percent of adsorbent material by volume. However, the adsorbent-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, configured in parallel and / or in series. Each of the conduits 254 (e.g., 256, 258, and 260) includes an outer conduit wall 262 circumferentially disposed around a flow path 264 (e.g., a fluid channel or orifice) along a central axis 266 from an inlet 268 to an outlet 270, wherein adsorbent material 272 is disposed along the inner surface 274 of the outer conduit wall 262 and / or along the outer surface 276 of a plurality of contactors 280 (e.g., contactor plates, panels, or fins). In the illustrated embodiment, the contactors 280 are arranged parallel to each other and parallel to the central axis 266. Each of the conduits 254 (e.g., 256, 258, and 260) may include a contactor assembly 278 having any number of contactors 280 (e.g., 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more contactors 280).

[0042] Each contactor in contactor 280 has a body 284 having an outer surface 276 disposed around an inner portion 286. In some embodiments, an adsorbent material 272 is disposed along the outer surface 276, while the inner portion 286 comprises a material 282 different from the adsorbent material 272. In some embodiments, the body 284 may be a solid body extending through the inner portion 286, wherein the body 284 extending through the inner portion 286 to the outer surface 276 is at least substantially or entirely made of the adsorbent material 272. In some embodiments, the body 284 may be a hollow body of the inner portion 286 (e.g., an inner chamber or cavity), wherein the body 284 has an outer wall 288 disposed around the inner portion 286. For example, the inner portion 286 may include a heat exchange loop or flow path extending through the body 284 between a fluid inlet and a fluid outlet, the heat exchange loop or flow path being coupled to a heat exchange loop for cooling and / or heating. In some embodiments, the internal portion 286 may be configured to circulate a cooling fluid during the adsorption mode of the adsorbent-based gas capture system 250, circulate a heating fluid (e.g., hot fluid 34 from the thermodynamic cycle 24) during the desorption mode, and circulate a cooling fluid during the cooling mode.

[0043] As discussed in detail below, the gas capture system 20 is configured to operate cyclically and repeatedly for each of the adsorbent-based gas capture units 252A, 252B, and 252C in the following sequence: (1) adsorption mode, (2) desorption mode, and (3) cooling mode. During the adsorption mode, the temperature of the adsorbent material 272 directly affects the adsorption efficiency of the adsorbent material 272. The adsorbent material 272 may have an optimal temperature or temperature range for the effective adsorption of unwanted gases. Unfortunately, the adsorption of unwanted gases into the adsorbent material 272 is an exothermic process that generates heat, which typically increases the temperature of the adsorbent material 272 and reduces its adsorption efficiency without any cooling. Therefore, the disclosed embodiments can control the cooling of the adsorbent material 272 during the adsorption mode to improve the adsorption efficiency. Similarly, the temperature of the adsorbent material 272 directly affects the desorption efficiency of the adsorbent material 272 during the desorption mode. The adsorbent material 272 may have an optimal temperature or temperature range for effective desorption of unwanted gases. Therefore, the disclosed embodiments allow for controlled heating of the adsorbent material 272 during desorption mode to improve desorption efficiency. As discussed in detail below, the controller 220 may be configured to control the WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140) to control the thermal fluid 34 supplied to each of the adsorbent-based gas capture units 252A, 252B, and 252C, individually or in combination with other heated fluids, during desorption mode.

[0044] The temperatures in the adsorption, desorption, and cooling modes can vary depending on the specific application. In some embodiments of carbon capture (e.g., CO2 capture), the adsorption mode can be configured to adsorb unwanted gases from gas 340 into adsorbent material 272 at a first temperature, the desorption mode can be configured to desorb unwanted gases from adsorbent material 272 using a heat source (e.g., hot fluid 34) at a second temperature, and the cooling mode can be configured to cool adsorbent 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 less than the first and second temperatures. For example, 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, and the third temperature may be less than or equal to approximately 0, 5, 10, 15, 20, 25, or 30 degrees Celsius.

[0045] In the illustrated embodiment, the gas capture system 20 includes a thermal control system 290 having a fluid circulation system 292, one or more fluid circulation loops 294 (e.g., fluid conduits, manifolds, valves, etc.), and one or more heat exchangers 296 coupled to each contactor assembly 278 in the adsorbent-based gas capture units 252A, 252B, and 252C. 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 may also 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 multiple components, such as components 300, 302, and 304, such as heat exchangers, pumps, valves, coolant suppliers, or any combination thereof. The thermal control system 290 circulates a hot fluid (e.g., a liquid or gaseous hot fluid) from the fluid circulation system 292 through the fluid circulation loop 294 and the heat exchanger 296 to exchange heat between the hot fluid and the contactor 280 and the adsorbent material 272 during any or all operating modes (e.g., adsorption mode, desorption mode, and / or cooling mode). In some embodiments, the fluid circulation loop 294 may include an independent fluid circulation loop for each contactor assembly in the contactor assembly 278, such that the thermal control system 290 can independently control the temperature of each contactor assembly in the contactor assembly 278 according to the operating modes (e.g., adsorption mode, desorption mode, and / or cooling mode) of the adsorbent-based gas capture units 252A, 252B, and 252C. For example, the thermal control system 290 is configured to circulate the hot fluid (e.g., circulate a coolant or cooling fluid at a relatively low temperature) during adsorption and cooling modes, thereby cooling the contactor 280 and the adsorbent material 272. For example, the thermal control system 290 is configured to circulate a hot fluid (e.g., circulate a heated fluid or heating fluid at a relatively high temperature) during desorption mode, thereby heating the contactor 280 and the adsorbent material 272 to facilitate desorption. As noted above, the hot fluid may include hot fluid 34 from the WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140) during desorption mode.

[0046] Adsorbent material 272 (e.g., a solid adsorbent) may cover, coat, or substantially line at least 50%, 60%, 70%, 80%, 90%, 95%, or 100% of the inner surface 274 of the outer conduit wall 262, the outer surface 276 of the contactor 280, and / or other structures within the conduit 254. In some embodiments, the contactor 280 may include a rectangular plate, an airfoil-shaped panel, parallel-arranged tubes, mesh-arranged tubes, multiple cylinders, radial protrusions, baffles, fins, honeycomb structures, bundled supported multiple contactor elements, or any combination thereof. The multiple contactor elements may include multiple particles, beads, strips, bundles, meshes, or other distributed structures that leave voids for fluid flow. Additionally or alternatively, adsorbent material 272 may at least partially fill or plug the internal volume of the central hole or inner surface 274, such that voids are retained to facilitate fluid flow (e.g., a porosity of less than or equal to 10%, 20%, 30%, 40%, or 50%). Furthermore, in some embodiments, the central axis 266 extending from the inlet 268 to the outlet 270 can define the flow path 264 as a linear flow path, a tortuous flow path, a winding or serpentine flow path, a spiral or helical flow path, a meandering flow path, an expanding and contracting flow path, a flow path with splitting and / or merging, or any combination thereof. For example, the flow path 264 can be defined as a tortuous flow path and include any number or configuration of the aforementioned flow paths.

[0047] Adsorbent material 272 may include one or more adsorbent materials configured to adsorb undesirable gases, such as those designed or suitable for adsorbing carbon oxides (CO). X Such as carbon dioxide (CO2) and carbon monoxide (CO), nitrogen oxides (NO) X ), sulfur oxides (SO X Adsorbent materials such as sulfur dioxide (SO2), methane (CH4), or any other undesirable gases or greenhouse gases restricted and / or considered by regulations as described herein. For example, adsorbent material 272 may comprise porous solid-phase materials, including mesoporous silica, zeolites (e.g., aluminosilicates), and metal-organic frameworks (MOFs) and covalent organic frameworks (COFs). The aforementioned adsorbent material 272 may be particularly suitable for CO2 adsorption in adsorbent-based gas capture units 252. However, any suitable adsorbent material 272 may be used, depending on the desired objective of capturing the undesirable gas. In some embodiments, multiple adsorbent-based gas capture systems 250 may be used in series, wherein each of the adsorbent-based gas capture systems 250 uses the same or different adsorbent material 272 to stage the removal and capture of the same or different undesirable gases.

[0048] The adsorbent-based gas capture system 250 can be configured to use a controller 220 and a sensor 222 to alternate between an adsorption mode (e.g., adsorbing unwanted gas into the adsorbent material 272), a desorption mode (e.g., desorbing unwanted gas from the adsorbent material 272), and a cooling mode (e.g., cooling the adsorbent material 272) for each of the adsorbent-based gas capture units 252A, 252B, and 252C associated with conduits 256, 258, and 260. The controller 220 is configured to control the adsorbent-based gas capture system 250 to perform interleaved operating cycles of the adsorbent-based gas capture units 252A, 252B, and 252C between different operating modes (e.g., adsorption mode, desorption mode, and cooling mode). For example, for a first duration, controller 220 may operate adsorbent-based gas capture unit 252A in adsorption mode, adsorbent-based gas capture unit 252B in desorption mode, and adsorbent-based gas capture unit 252C in cooling mode. As a further example, for a second duration, controller 220 may operate adsorbent-based gas capture unit 252A in desorption mode, adsorbent-based gas capture unit 252B in cooling mode, and adsorbent-based gas capture unit 252C in adsorption mode. As a further example, for a third duration, controller 220 may operate adsorbent-based gas capture unit 252A in cooling mode, adsorbent-based gas capture unit 252B in adsorption mode, and adsorbent-based gas capture unit 252C in desorption mode. The adsorbent-based gas capture system 250 can also be configured to simultaneously operate multiple units (e.g., two, three, four, or more) of the adsorbent-based gas capture unit 252 in each operating mode, such as multiple units 252 in adsorption mode, multiple units 252 in desorption mode, and multiple units 252 in cooling mode. The multiple units 252 can be arranged in series, in parallel, or in a combination thereof. The controller 220 is configured to alternate between adsorption mode, desorption mode, and cooling mode via multiple support systems.

[0049] The support system may include a 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 a gas inlet system), a heating fluid supply system 316 (e.g., a heated gas and / or heated liquid supply system), and a cooling fluid supply system 318, while the downstream flow distribution system 312 includes an adsorption post-treatment system 320 (e.g., after adsorption mode), a desorption post-treatment system 322 (e.g., a fluid processing system after desorption mode), and a cooling post-treatment system 324 (e.g., after cooling mode).

[0050] The gas supply system 314 of the upstream flow distribution system 310 is configured to supply gas 340 (e.g., air 190 and / or other gases) to achieve adsorption mode when each of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) is selectively operated in adsorption mode via controller 220. Although the illustrated embodiment is directed towards... Figure 1 The DAC system 18, however, may include exhaust gas, flue gas, or other combustion gases, either alone or in combination with air 190. The gas supply system 314 includes a gas pretreatment system 330 having one or more gas pretreatment components 332, 334, and 336, configured to treat, adjust, and / or control the characteristics of gas 340 upstream of ducts 254 (e.g., 256, 258, and 260) of adsorbent-based gas capture units 252 (e.g., units 252A, 252B, and 252C). For example, the gas pretreatment component 332 may include thermal control components (e.g., gas temperature control components), such as heat exchangers, heaters, coolers, or any combination thereof, configured to regulate (e.g., increase or decrease) the temperature of gas 340. The heat exchanger may exchange heat with one or more of water, exhaust gas, compressor vents, waste heat, heat source 26, or some other hot fluid. In some embodiments, a waste heat recovery system may be used for heat transfer in the heat exchanger. Gas pretreatment component 334 may include pressure control components such as a pressure regulator, expander or expansion chamber, contractor or contraction chamber, energy-increasing fan or pump, energy-extracting turbine, or other suitable pressure controller. Gas pretreatment component 336 may include one or more contaminant removal units such as particulate filters, moisture removal units or dryers, chemical removal units, and / or other removal units configured to clean gas 340. For example, gas pretreatment component 336 may include a humidity controller configured to maintain a desired relative humidity of gas 340 received in the adsorbent-based gas capture system 250.

[0051] The gas supply system 314 may also include one or more valves 342 configured to control the distribution of gas 340 to multiple conduits 254 (e.g., 256, 258, and 260) of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 344, 346, and 348. For example, valves 342 may include one or more multi-way valves and / or distribution manifolds to independently distribute gas 340 to the respective adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 344, 346, and / or 348 when operating in adsorption mode in response to a control signal from controller 220.

[0052] The heating fluid supply system 316 of the upstream flow distribution system 310 is configured to supply heating fluid to enable desorption mode when each of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) is selectively operated in desorption mode via controller 220. As discussed in further detail below, the heating fluid supply system 316 may also cooperate with the vacuum system of the desorption post-processor 442. The heating fluid supply system 316 includes one or more heating fluid suppliers 350, such as one or more steam suppliers, hot water suppliers, heated gas suppliers, and / or waste heat suppliers. The heating fluid may also be described as a purge fluid, such as purge gas or purge steam. For example, the heating fluid supplier 350 may include a steam turbine system 14, a steam generation system 16, a WHR system 22 (e.g., a thermodynamic cycle 24 and a heat storage system 140), a waste heat recovery system (e.g., recovering heat from a compressor, pump, generator, reactor, or other power plant equipment), or any combination thereof. The heating fluid supplier 350 may be configured to supply heating fluid 352 (e.g., steam and / or heated water) and / or heating fluid 354 (e.g., waste heat recovery fluid such as hot fluid 34) to the heating fluid control 356 of the heating fluid supply system 316. In some embodiments, heating fluid 352 and / or 354 may comprise heated liquids and / or heated gases, such as heated CO2, air, inert gases such as nitrogen, rare gases, water, oil, or any combination thereof. In some embodiments, the thermodynamic cycle 24 uses waste heat recovered from the thermal power generation system 28 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) via the WHR system 22 and provides hot fluid 34 for use as heating fluid 354. Hot fluid 34 (e.g., waste heat recovery fluid) may also be described as excess heat or waste heat recovered for use in the heating fluid supply system 316 of the adsorbent-based gas capture unit 252. In some embodiments, the heat storage system 140 stores waste heat and / or provides waste heat as a heat fluid 34 for use as a heating fluid 354.

[0053] Heating fluid control unit 356 includes one or more heating fluid control components 358, 360, and 362, which can be configured to process, adjust, and / or control the characteristics of heating fluid 352 and / or heating fluid 354 upstream of conduits 254 (e.g., 256, 258, and 260) of adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C). For example, heating fluid control component 358 may include thermal control components (e.g., temperature control components), such as heat exchangers, heaters, coolers, or any combination thereof, configured to regulate (e.g., increase or decrease) the temperature of heating fluid 352 and / or heating fluid 354. The heat exchanger may exchange heat with water, lubricant, coolant, refrigerant, or some other hot fluid. In some embodiments, a waste heat recovery system may be used for heat transfer in the heat exchanger. The heating fluid control unit 360 may include pressure control components, such as a pressure regulator, expander or expansion chamber, contractor or contraction chamber, energy-increasing fan or pump, energy-extracting turbine, or other suitable pressure controller. The heating fluid control unit 362 may include pretreatment components, such as particulate filters, cold water discharge devices, and / or other pretreatment components configured to alter the properties of heating fluids 352 and / or 354 or remove contaminants.

[0054] The heating fluid supply system 316 may also include one or more valves 364 configured to control the distribution of heating fluid 352 (e.g., steam and / or heated water) and / or heating fluid 354 (e.g., waste heat recovery fluid) to multiple conduits 254 (e.g., 256, 258, and 260) of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 366, 368, and 370. For example, valve 364 may include one or more multi-way valves and / or distribution manifolds to independently distribute heating fluid 352 and / or heating fluid 354 to the respective adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 366, 368, and 370 when operating in desorption mode in response to a control signal from controller 220.

[0055] The cooling fluid supply system 318 of the upstream flow distribution system 310 is configured to supply cooling fluid to achieve a cooling mode when each of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) is selectively operated in a cooling mode via the controller 220. The cooling fluid supply system 318 includes one or more cooling fluid suppliers 372, such as one or more water suppliers, cooled air suppliers, cooled inert gas (e.g., nitrogen) suppliers, cooled CO2 suppliers, or any combination thereof. The cooling fluid suppliers 372 may be configured to supply coolant or cooling fluid 374 (e.g., liquid or gaseous coolant) to the cooling fluid control 376 of the cooling fluid supply system 318.

[0056] Cooling fluid control component 376 includes one or more cooling fluid control components 378, 380, and 382, ​​which can be configured to process, adjust, and / or control the characteristics of cooling fluid 374 upstream of conduits 254 (e.g., 256, 258, and 260) of adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C). For example, cooling fluid control component 378 may include thermal control components (e.g., temperature control components), such as heat exchangers, heaters, coolers, or any combination thereof, configured to regulate (e.g., increase or decrease) the temperature of cooling fluid 374. Heat exchangers may exchange heat with water, lubricants, coolants, refrigerants, or some other hot fluid. Cooling fluid control component 380 may include pressure control components, such as pressure regulators, expanders or expansion chambers, contractors or contraction chambers, energy-increasing fans or pumps, energy-extracting turbines, or other suitable pressure controllers. The cooling fluid control unit 382 may include pretreatment components, such as particulate filters and / or other pretreatment components configured to change the properties of the cooling fluid 374 or remove contaminants.

[0057] The cooling fluid supply system 318 may also include one or more valves 384 configured to control the distribution of cooling fluid 374 (e.g., liquid or gaseous coolant) to multiple conduits 254 (e.g., 256, 258, and 260) of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 386, 388, and 390. For example, valve 384 may include one or more multi-way valves and / or distribution manifolds to independently distribute cooling fluid 374 to the respective adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) via distribution conduits 386, 388, and 390 when operating in cooling mode in response to a control signal from controller 220.

[0058] In the illustrated embodiment, controller 220 is configured to control upstream flow distribution system 310 to alternately distribute the flow rates of gas 340 during adsorption mode, heating fluid 352 and / or heating fluid 354 during desorption mode, and cooling fluid 374 during cooling mode to different adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) having adsorbent material 272. In adsorption mode, gas 340 (e.g., air 190 and / or other gases) flows through conduit 254 of the selected adsorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) and contacts the adsorbent material 272 disposed on the inner surface 274 of the outer conduit wall 262 and / or the outer surface 276 of the contactor 280, such that the adsorbent material 272 adsorbs unwanted gases (e.g., CO2) from gas 340. In some embodiments, the thermal control system 290 may circulate coolant through the heat exchanger 296 to provide cooling to the contactor 280 and the adsorbent material 272 during adsorption mode. The thermal control system 290 may also facilitate heat transfer to the coolant via multiple heat pipes 298 of the heat exchanger 296. The adsorbent-based gas capture unit 252 then discharges the treated gas 400 (e.g., lean or substantially free of unwanted gases) to the adsorption post-treatment system 320.

[0059] In desorption mode, heating fluid 352 and / or heating fluid 354 flow through conduit 254 of a selected adsorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) and contact adsorbent material 272 disposed on the inner surface 274 of the outer conduit wall 262 and / or the outer surface 276 of the contactor 280, thereby heating the adsorbent material 272 to facilitate the desorption of unwanted gases (e.g., CO2) from the adsorbent material 272. In some embodiments, the desorption mode may be configured to indirectly heat the adsorbent material 272 via a heating circuit (e.g., a heating conduit) extending through the adsorbent-based gas capture unit 252. For example, thermal control system 290 may circulate heating fluid (e.g., heating fluid 352 and / or heating fluid 354) through heat exchanger 296 to provide heating of contactor 280 and adsorbent material 272. As noted above, heating fluid 354 may include hot fluid 34 from thermodynamic cycle 24. The thermal control system 290 also facilitates heat transfer from the heating fluid across the contactor 280 via multiple heat pipes 298 of the heat exchanger 296. The adsorbent-based gas capture unit 252 then discharges a fluid flow 402 comprising the unwanted gas, the heating fluid 352, and / or the heating fluid 354 for further processing by the desorption post-treatment system 322.

[0060] In cooling mode, cooling fluid 374 flows through conduit 254 of a selected adsorbent-based gas trapping unit 252 (e.g., 252A, 252B, or 252C) and contacts adsorbent material 272 disposed on the inner surface 274 of the outer conduit wall 262 and / or the outer surface 276 of the contactor 280, thereby cooling the adsorbent material 272 and the contactor 280. In some embodiments, the cooling mode may be configured to indirectly cool the adsorbent material 272 and the contactor 280 via a cooling circuit (e.g., a cooling conduit) extending through the adsorbent-based gas trapping unit 252. For example, thermal control system 290 may circulate cooling fluid through heat exchanger 296 to provide cooling to the contactor 280 and the adsorbent material 272. Thermal control system 290 may also facilitate the transfer of heat from the contactor 280 and the adsorbent material 272 via a plurality of heat pipes 298 of heat exchanger 296. The cooling mode is configured to cool and regenerate the adsorbent material 272 prior to the subsequent adsorption mode. The adsorbent-based gas capture unit 252 then discharges a fluid stream 404 (e.g., cooling fluid 374) for processing by the cooled system 324.

[0061] In some embodiments, the adsorbent-based gas capture system 250 includes a movable adsorbent system configured to continuously or periodically move adsorbent material 272 between adsorption, desorption, and cooling modes. For example, the adsorbent-based gas capture system 250 may include a rotary contactor assembly or wheel (e.g., a rotary contactor having adsorbent material 272) configured to rotate from adsorption, desorption, and cooling, thereby providing a continuous flow of captured undesirable gas. For example, the wheel (e.g., a rotary contactor having adsorbent material 272) may extend into each of a plurality of conduits 254 and rotate continuously through the conduits 254. During wheel rotation, one or more conduits in conduit 254 flow the gas 340 to be treated to remove unwanted gases, while simultaneously flowing heating fluid 352 and / or heating fluid 354 to remove and capture unwanted gases (e.g., CO2), thereby generating captured gas 204. Simultaneously, one or more conduits in conduit 254 also flow cooling fluid 374 to regenerate adsorbent material 272. For desorption, heating fluid 352 and / or heating fluid 354 may be delivered or generally configured to provide direct and / or indirect heat transfer to adsorbent material 272, thereby aiding in the separation and capture of unwanted gases.

[0062] In an illustrated embodiment, controller 220 is configured to control downstream flow distribution system 312 to alternately distribute flows from each adsorbent-based gas capture unit 252 (e.g., 252A, 252B, and 252C), thereby delivering treated gas 400 to adsorption post-treatment system 320 during adsorption mode, delivering fluid flow 402 (e.g., unwanted gas, heating fluid 352, and / or heating fluid 354) to desorption post-treatment system 322 during desorption mode, and delivering fluid flow 404 (e.g., cooling fluid 374) to cooling post-treatment system 324 during cooling mode. In some embodiments, downstream flow distribution system 312 includes one or more valves 410 fluidly coupled to adsorbent-based gas capture unit 252A, one or more valves 412 fluidly coupled to adsorbent-based gas capture unit 252B, and one or more valves 414 fluidly coupled to adsorbent-based gas capture unit 252C. Valve 410 may include one or more multi-way valves and / or distribution manifolds connected to distribution conduits 416, 418, and 420, which are respectively connected to the adsorption post-treatment system 320, the desorption post-treatment system 322, and the cooling post-treatment system 324. Valve 412 may include one or more multi-way valves and / or distribution manifolds connected to distribution conduits 422, 424, and 426, which are respectively connected to the adsorption post-treatment system 320, the desorption post-treatment system 322, and the cooling post-treatment system 324. Valve 414 may include one or more multi-way valves and / or distribution manifolds connected to distribution conduits 428, 430, and 432, which are respectively connected to the adsorption post-treatment system 320, the desorption post-treatment system 322, and the cooling post-treatment system 324. In operation, controller 220 is configured to control valves 410, 412 and 414 to independently control the flow rates from the adsorbent-based gas capture unit 252 (e.g. 252A, 252B and 252C) to the adsorption post-treatment system 320 in adsorption mode, to the desorption post-treatment system 322 in desorption mode and to the cooling post-treatment system 324 in cooling mode.

[0063] The adsorption post-treatment system 320 includes a treated gas treatment system 440, which may include a gas exhaust outlet or chimney, an additional gas treatment system, or any other suitable post-treatment equipment. In some embodiments, the adsorption post-treatment system 320 may combine multiple exhaust gases into a single outlet or chimney. In some embodiments, when gas 340 is air 190, the treated gas may be used for ventilation and / or other uses that benefit from the treated air.

[0064] The desorption post-treatment system 322 may include a desorption post-processor 442 having one or more desorption post-treatment components 444, 446, and 448. In some embodiments, the fluid flow 402 directed to the desorption post-processor 442 is a result of a desorption mode in which heated fluid 352 (e.g., steam and / or heated water) and / or heated fluid 354 (e.g., waste heat recovery fluid such as hot fluid 34) are directed through conduits 254 of the adsorbent-based gas capture unit 252 (e.g., 252A, 252B, or 252C) to desorb unwanted gases (e.g., CO2) from the adsorbent material 272. Therefore, one or more desorption post-treatment components 444, 446, and 448 (e.g., steam, heated water, and / or other fluid processing components) may be configured to process, adjust, and / or control the characteristics of fluid flow 402 (e.g., steam, heated water, and / or other fluid flow) from conduits 254 (e.g., 256, 258, and 260) of the adsorbent-based gas capture unit 252 (e.g., 252A, 252B, and 252C). For example, desorption post-treatment component 444 may include a captured gas / heated fluid separator configured to separate heated fluid 352 (e.g., steam and / or heated water) and / or heated fluid 354 from the captured gas, thereby outputting fluid 450 (e.g., water condensate or other separated fluid) and captured gas 204. Examples of captured gas / heated fluid separators include thermal control components, pressure control components, chemical separation components, or combinations thereof. For example, the captured gas / heated fluid separator may be configured to use a condenser to condense or cool the heated fluid 352 (e.g., steam). The desorption post-treatment component 446 may include one or more removal units configured to remove contaminants from the fluid 450 and / or captured gas 204. For the fluid 450, the removal unit may include a particulate filter and / or a water treatment unit. For the captured gas 204, the removal unit may include a particulate filter, a water removal unit, a dryer, or an additional gas treatment unit. The desorption post-treatment 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 desorption post-treatment component 448 may also include a vacuum system with one or more vacuum pumps configured to draw the captured gas / heated fluid stream from the adsorbent-based gas capture unit 252. In other words, the vacuum pumps are configured to create a low-pressure environment to aid in drawing the captured gas / heated fluid stream from the adsorbent-based gas capture unit 252.

[0065] The cooling system 324 may include a cooling fluid recirculation system 452 configured to recirculate fluid flow 404 back to the cooling fluid supply system 318 as 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, cooling system, and flow control valve. The cooling system may include a heat exchanger configured to transfer heat from fluid flow 404, thereby cooling the fluid flow for reuse as cooling fluid 374. In some embodiments, heat available from fluid flow 404 may be recovered in one or more heat exchangers to heat heating fluid 352 and / or heating fluid 354 in heating fluid supply system 316, thereby reducing total heating energy requirements. Excess low-grade heat from fluid flow 404 may then be discharged into the environment.

[0066] Controller 220 is configured to receive feedback from sensor 222 to adjust various operating parameters and change the operating mode (e.g., adsorption mode, desorption mode, and cooling mode) of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C). For example, controller 220 may be configured to alternate the flow (e.g., gas 340, heating fluid 352, and / or heating fluid 354 and cooling fluid 374) through multiple conduits 254 (e.g., 256, 258, and 260), such that the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C) can alternate between adsorption mode, desorption mode, and cooling mode. In adsorption mode, conduit 254 receives the flow of gas 340, adsorbs unwanted gases (e.g., CO2) from gas 340 into adsorbent material 272, and outputs treated gas 400 with reduced content or concentration level of unwanted gases. The adsorption of unwanted gases into the adsorbent material 272 is an exothermic process that generates heat. A thermal control system 290, including a heat exchanger 296 and a heat pipe 298, helps regulate the temperature of the adsorbent material 272 during adsorption mode, thereby maintaining or increasing the adsorption efficiency of the adsorbent material 272. In desorption mode, the conduit 254 receives a flow of heated fluid 352 (e.g., steam and / or heated water) and / or heated fluid 354, desorbing unwanted gases (e.g., CO2) from the adsorbent material 272 into the heated fluid 352 and / or heated fluid 354, and outputs a fluid flow 402 containing the desorbed unwanted gases (e.g., heated fluid 352 and / or heated fluid 354 rich in unwanted gases such as CO2). The desorption of unwanted gases from the adsorbent material 272 is an endothermic process, and the heated fluid 352 and / or heated fluid 354 provides sufficient heat (e.g., directly or indirectly) to drive the desorption of unwanted gases (e.g., CO2) from the adsorbent material 272. In cooling mode, conduit 254 receives a flow of cooling fluid 374 (e.g., gaseous or liquid coolant), thereby cooling adsorbent material 272 and contactor 280.

[0067] Controller 220 is configured to monitor sensors 222, such as sensors 222 located at or upstream of inlet 266 and sensors 222 located at or downstream of outlet 268, to assess the rates of adsorption, desorption, and cooling, the concentration levels of unwanted gases, and other characteristics affecting the operating modes of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C). If sensors 222 indicate a need to alternate the operating modes (e.g., adsorption, desorption, and cooling modes) of the adsorbent-based gas capture units 252 (e.g., 252A, 252B, and 252C), controller 220 may be configured to control valves 342, 364, 384, 410, 412, and 414 to change the flow rate through conduit 254 to support the desired operating mode. Sensor 222 can also monitor the temperature of adsorbent material 272 and adjust thermal control system 290 according to the operating mode to provide heating or cooling (e.g., cooling during adsorption and cooling mode and heating during desorption mode).

[0068] For gas 340 treated in one of the conduits 254 in adsorption mode, controller 220 may be configured to control gas pretreatment system 330 to control the characteristics of gas 340 (e.g., temperature, pressure, flow rate, etc.). Similarly, controller 220 is configured to control treated gas treatment system 440 to control the treatment of treated gas 400 discharged from one or more conduits in conduits 254. For heated fluid 352 (e.g., steam and / or heated water) and / or heated fluid 354 (e.g., waste heat recovery fluid such as heated fluid 34) supporting desorption mode in one of the conduits 254, controller 220 may be configured to control steam generation system 16, steam turbine system 14, WHR system 22 (e.g., thermodynamic cycle 24 and heat storage system 140), heated fluid control element 356, or any combination thereof, to control the characteristics of heated fluid 352 and / or heated fluid 354 (e.g., temperature, pressure, flow rate, steam content, water content, etc.). Similarly, controller 220 is configured to control desorption post-processor 442 to control the treatment of fluid flow 402 (including undesirable gases desorbed during desorption mode) exiting from one or more conduits in conduit 254. For cooling fluid 374 supporting a cooling mode in one of conduits 254, controller 220 may be configured to control cooling fluid control element 376 and / or cooling fluid recirculation system 452 to control the characteristics of cooling fluid 374 (e.g., temperature, pressure, flow rate, etc.). Similarly, controller 220 is configured to control cooling fluid recirculation system 452 to control the treatment of fluid flow 404 (e.g., cooling fluid 374) exiting from one or more conduits in conduit 254.

[0069] Figure 3 yes Figure 1 A schematic diagram of an embodiment of the combined circulation system 10 illustrates 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 to capture undesirable gases. Example solvents include monoethanolamine (MEA), diethylene glycolamine (DGA), higher amine solvents, amino acid salts, carbonate solvents, ammonia, immiscible liquids, and ionic liquids. As discussed below, 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 thermal storage system 140). For example, the heated fluid 502 may include steam and / or heated water 501, 503 from the steam turbine system 14 and / or the steam generation system 16. By another example, the heated fluid 502 may include heated gases and / or heated liquids (e.g., heat fluid 34) from the thermodynamic cycle 24 of the WHR system 22 and / or the thermal storage system 140. As discussed above, the thermodynamic cycle 24 is driven by waste heat recovered from the thermal power generation system 28 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54), and the waste heat is extracted as heat fluid 34 for use in one or more gas capture systems 20 of the DAC system 18 (e.g., solvent-based gas capture system 500).

[0070] The power generation system 12, steam turbine system 14, steam generation system 16, and WHR system 22 (including thermodynamic cycle 24 and thermal storage system 140) are substantially the same as those discussed in detail above. In some embodiments, the gas capture system 20 (e.g., solvent-based gas capture system 500) may be configured to deliver heated fluid 502 (e.g., steam and / or heated water 501, 503) from steam turbine system 14 and / or steam generation system 16 to gas capture system 20 (e.g., solvent-based gas capture system 500), wherein the steam may be high-pressure steam, medium-pressure steam, and / or low-pressure steam extracted from one or more sections of steam generation system 16 and / or one or more steam turbines of steam turbines 80, 82, and 84 of steam turbine system 14. Additionally or alternatively, in some embodiments, the heated fluid 502 (e.g., the hot fluid 34) may be supplied by the WHR system 22 (e.g., the thermodynamic cycle 24 and / or the thermal storage system 140) to the gas capture system 20 (e.g., the solvent-based gas capture system 500).

[0071] The solvent-based gas capture system 500 includes an absorber 504 (e.g., an absorber tower), a stripper 506 (e.g., a stripper column), a gas circuit 508 (e.g., a gas processing circuit), a solvent circuit 510 (e.g., a fluid absorbent circuit), and one or more heated fluid circuits 512. Each of the gas circuit 508, solvent circuit 510, and heated fluid circuit 512 includes one or more fluid conduits or lines, fluid manifolds, fluid separators, fluid combiners, fluid mixing chambers, fluid valves, internal fluid paths through components, or any combination thereof. In operation, the gas circuit 508 is configured to deliver air 190 (or any other gas flow having an undesired gas) through the absorber 504, while the solvent circuit 556 is configured to deliver a solvent flow through the absorber 504 and the stripper 506. Gas circuit 508 includes a gas path 514 extending toward absorber 504 between absorber 504 and WHR system 22 and / or steam generation system 16, a gas path 516 extending upward through absorber 504, and a gas path 518 extending away from absorber 504. Solvent circuit 510 extends in a loop through absorber 504 and stripper 506, including a solvent path 520 extending downward through absorber 504, a solvent path 522 extending from absorber 504 to stripper 506, a solvent path 524 extending downward through stripper 506, and a solvent path 526 extending from stripper 506 to absorber 504. Heated fluid circuit 512 extends between stripper 506 and one or more heated fluid sources 528 to support operation of stripper 506 using heated fluid 502. The heated fluid loop 512 may be configured to extract the heated fluid 502 at pressures and temperatures suitable for transferring heat to the stripper 506, thereby reducing or eliminating the need for a separate heat source for the stripper 506. In some embodiments, the heated fluid loop 512 may be configured to supply high-pressure steam, medium-pressure steam, and / or low-pressure steam (e.g., steam 501, 503) from the steam turbine system 14 and / or the steam generation system 16 to the stripper 506 as a heated fluid source 528. In an illustrated embodiment, the heated fluid source 528 includes a WHR system 22 (e.g., thermodynamic cycle 24 and / or heat storage system 140) as a source of the heated fluid 502 (e.g., hot fluid 34).

[0072] The heated fluid loop 512 may include any number and configuration 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 loop 512 may be fluidly and mechanically coupled to the heated fluid source 528 at one or more heated fluid extraction locations 530 (e.g., extraction ports or connections). For example, heated fluid extraction locations 530 may be located at one or more locations along the thermodynamic cycle 24. In some embodiments, 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 at sections of the steam generation system 16 (e.g., high-pressure, medium-pressure, and low-pressure) with steam turbines 80, 82, and 84, upstream, downstream, and / or between that section and the steam turbine. Additionally, the heated fluid circuit 512 may be fluidly and mechanically coupled to the stripper 506 at one or more heated fluid injection locations 532 (e.g., injection ports or connections). In the illustrated embodiments, the heated fluid injection locations 532 may be located 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 heated fluid circuits in the heated fluid circuit 512 with any combination of heated fluid extraction locations 530 and heated fluid injection locations 532. The heated fluid circuit 512 may be a separate circuit (e.g., a separate heated fluid path or conduit) or an interconnected circuit (e.g., a fluidly coupled heated fluid path or conduit) with one or more common conduits, wherein the heated fluid circuit 512 may include one or more valves 534 coupled to the controller 220 for selectively controlling the flow of heated fluid to the stripper 506.

[0073] In the illustrated embodiment, the heated fluid loop 512 includes one or more heated fluid loops 536 between the WHR system 22 (e.g., thermodynamic cycle 24 and / or heat storage system 140) and the stripper 506. The one or more heated fluid loops 536 are fluidly and mechanically coupled to the WHR system 22 (e.g., thermodynamic cycle 24 and / or heat storage system 140) at one or more heated fluid extraction locations 530, and the one or more heated fluid loops 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). In some embodiments, the heated fluid loop 512 may include one or more heated water and / or steam loops extending between the stripper 506 and one or more sections (e.g., high-pressure, medium-pressure, and low-pressure) of the steam generation system 16, one or more heated water and / or steam loops extending between the stripper 506 and one or more steam turbines of the steam turbines 80, 82, and 84 of the steam turbine system 14, or any combination thereof. In some embodiments, the heated fluid extraction location 530 may include multiple different locations, and the heated fluid injection locations 532 (e.g., 540, 542, 544, and 546) may include multiple different locations. However, the heated fluid loop 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. In some embodiments, each of the heated fluid circuits 512 may be selectively coupled 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 control elements. The heated fluid circuits 512 are configured to supply heated fluid 502 to the stripper 506 along their respective circuits at a temperature, pressure, and flow rate controlled at least in part by valves 534 (e.g., via controller 220 and feedback control from sensor 222). Additional details regarding the heated fluid circuits 512 and the supply of heated fluid to the stripper 506 will be discussed below.

[0074] Absorber 504 includes multiple absorber sections 560 disposed within a container or housing 562, wherein housing 562 includes a gas inlet 564, a gas outlet 566, a solvent inlet 568, and a solvent outlet 570. Housing 562 has a top portion 572, a bottom portion 574, and an intermediate portion 576 axially disposed between the top portion 572 and the bottom portion 574 relative to a central axis 578 of housing 562. Top portion 572 includes a top plate or cover 580 having a gas outlet 566 coaxial with the central axis 578. However, gas outlet 566 may be disposed off-center from the central axis 578 or at other locations along top portion 572. Intermediate portion 576 includes sidewalls 582 extending about the central axis 578. For example, sidewall 582 may be an annular sidewall, square sidewall, rectangular sidewall, or any other suitable shape extending about the central axis 578. In some embodiments, gas outlet 566 may be disposed in sidewall 582 along top portion 572. Additionally, a solvent inlet 568 may be disposed in the top portion 572 along a top plate or cover 580 or a sidewall 582. A bottom portion 574 may include a substrate 584 located below the gas inlet 564 and the solvent outlet 570. In an illustrated embodiment, the gas inlet 564 and the solvent outlet 570 are disposed along the bottom portion 574 in the sidewall 582. However, in some embodiments, the gas inlet 564 and / or the solvent outlet 570 may be disposed in the substrate 584 within the bottom portion 574. In some embodiments, the gas inlet 564 may include multiple gas inlets and / or the solvent outlet 570 may include multiple solvent outlets.

[0075] The plurality of absorber sections 560 within the internal volume 586 of the housing 562 may include any number and type of absorber sections 560, such as absorber sections 588, 590, 592, 594, 596, and 598. These absorber sections may include packing material, support trays or screens, wire mesh, solvent dispensers, or any combination thereof in any configuration. For example, each packing material may include a plurality of beads, balls, or mixture-inducing structures configured to facilitate mixing between the gas flow and the solvent flow in absorber 504. Each support tray or screen may include wire mesh, a plate with multiple openings, or another suitable structure that holds the packing material in place while allowing fluid flows of gas and solvent to pass through the support tray or screen in opposite directions through absorber 504. Each solvent dispenser may include a plurality of solvent nozzles configured to dispense solvent across internal volume 586. In some embodiments, absorber sections 588, 592, 596, and 598 include wire mesh, while absorber sections 590 and 594 include packing material, support trays or screens, and solvent dispensers. However, absorber sections 560 (e.g., 588, 590, 592, 594, 596, and 598) are not limited to the illustrated configurations.

[0076] In operation, absorber 504 is configured to create cross-flow or counter-flow of gas 600 (e.g., air 190 and / or other gases) along gas path 516 and lean solvent 602 along solvent path 520 within internal volume 586, thereby facilitating the absorption of certain undesirable gases (e.g., CO2) from gas 600 into lean solvent 602. As shown, at bottom portion 574, gas 600 enters absorber 504 through gas inlet 564 and flows upward through internal volume 586 of absorber 504. Gas 600 entering absorber 504 through gas inlet 564 can form gas bubbles that rise upward through lean solvent 602 within internal volume 586. Gas 600 then passes through each subsequent absorber section 560 (e.g., 588, 590, 592, 594, 596, and 598).

[0077] At the intermediate section 576 (or top section 572), the solvent-based gas capture system 500 supplies lean gas solvent 602 into the internal volume 586 using one or more solvent dispensers (such as solvent distribution manifolds, solvent nozzles, or solvent injector grids). The solvent-based gas capture system 500 may supply lean gas solvent 602 directly at, above, and / or below absorber section 560 via the illustrated solvent inlet 568 or any number or arrangement of solvent inlets 568. The lean gas solvent 602 then flows downward through the internal volume 586 through each subsequent absorber section 560. As the lean gas solvent 602 passes through each absorber section 560, various mixing structures (e.g., packing, wire mesh, support trays, etc.) are configured to aid in mixing the lean gas solvent 602 with the gas 600, thereby facilitating the absorption of various undesirable gases from the gas 600 into the lean gas solvent 602. For example, the lean gas solvent 602 can be configured to absorb carbon dioxide (CO2) or other undesirable gases, as discussed in detail above. When the absorption process occurs, heat is generated within the absorber 504, thereby raising the temperature of the solvent within the absorber 504.

[0078] In some embodiments, a thermal control system 604 may be coupled to the absorber 504 to control the temperature and improve the efficiency of the absorption process. For example, 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., a cooler) and a pump 610. The pump 610 is configured to circulate the 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.

[0079] In some embodiments, absorber 504 further includes a water washing system 612 having a heat exchanger 614 (e.g., a cooler) and a pump 616 disposed along a water washing loop 618. In some embodiments, absorber sections 594, 596, and / or 598 may be configured to assist the water washing process of the water washing system 612, while absorber sections 588, 590, and 592 help enhance the mixing between gas 600 and lean gas solvent 602 to increase the absorption of unwanted gases. For example, absorber sections 594, 596, and / or 598 may be configured to help distribute water across absorber 504 in a top portion 572 for removing any soluble solvents from the gas 600 flowing upward through absorber 504. In some embodiments, the water washing system 612 may be eliminated or moved downstream of absorber 504.

[0080] Finally, absorber 504 discharges the gas-rich solvent 620 at the bottom portion 574 through solvent outlet 570, and the treated gas 622 at the top portion 572 through gas outlet 566. The treated gas 622 may be substantially free of or vaporize one or more undesirable gases (e.g., CO2). In contrast, the gas-rich solvent 620 may have absorbed one or more undesirable gases (e.g., CO2). Therefore, 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 specific gas absorption occurring in absorber 504). Similarly, gas 600 may be described as containing or being rich in CO2 (or containing or being rich in other gases, depending on the undesirable gas), while the treated gas 622 may be described as a CO2-reduced, lean, or non-containing gas (or other reduced, lean, or non-containing gas, depending on the undesirable gas and the specific gas absorption occurring in absorber 504). The gas absorption discussed herein is intended to cover any one or more undesirable gases or any other regulated gases or greenhouse gases described herein.

[0081] In some embodiments, gas circuit 508 may include one or more components upstream of absorber 504. For example, when processing air 190, gas circuit 508 may include one or more compressors 210 configured to compress air 190 upstream of absorber 504. By another example, gas circuit 508 may include a gas cooler or gas cooling system, such as a direct contact cooler (DCC) 624, disposed upstream of absorber 504 along gas path 514. In some embodiments, DCC 624 may be scaled down or eliminated in solvent-based gas capture system 500. If included in gas circuit 508, DCC 624 may include a cooling housing 626 housing 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 may also include a cooling fluid circuit 634 having a pump 636 and a heat exchanger 638 (e.g., a cooler), wherein the cooling fluid circuit 634 is coupled above the wire mesh 628 to the cooling fluid distributor 630 and below the wire mesh 628 to the bottom portion of the housing 626. The pump 636 is configured to circulate 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 it to another working fluid. Multiple fluid nozzles 632 distribute the cooling fluid across the internal volume of the housing 626 (e.g., a cooling fluid dispersion), while the DCC 624 delivers a gas flow from a gas inlet 640 to a gas outlet 642, as indicated by arrow 644. Thus, the cooling fluid dispersion directly contacts and cools the gas flow (e.g., air 190 and / or other gases). In some embodiments, the gas circuit 508 also includes one or more compressors and / or fans 646 configured to increase the pressure and / or flow rate of the gas stream (e.g., air 190 and / or other gases) supplied to the absorber 504.

[0082] The solvent-based gas capture system 500 may further include multiple components of a solvent circuit 510 along the absorber 504 and stripper 506. In an illustrated embodiment, the solvent circuit 510 includes a pump 648, a heat exchanger 650, and a heat exchanger 704 along a solvent path 522 from the absorber 504 to the stripper 506, and the solvent circuit 510 includes a pump 652, a heat exchanger 650, a heat exchanger 654, and a filter 656 along a solvent path 526 from the stripper 506 to the absorber 504. The pump 648 is configured to pump a rich gas solvent 620 along the solvent path 522 through heat exchangers 650 and 704 to the stripper 506, while the pump 652 is configured to pump a lean gas solvent 602 along the solvent path 526 through heat exchangers 654 and 656 and the filter 656 to the absorber 504. Heat exchanger 650 is configured to transfer heat away from lean solvent 602 in solvent path 526 to rich solvent 620 in solvent path 522, thereby cooling lean solvent 602 and heating rich solvent 620. As discussed in further detail below, heat exchanger 704 is configured to transfer heat from heated fluid 502 in heated fluid circuit 702 to rich solvent 620 in solvent path 522, thereby heating rich solvent 620. Heat exchanger 654 is configured to cool lean solvent 602 by transferring heat away from lean solvent 602 to a coolant stream (e.g., water or other liquid coolant), thereby providing cooled lean solvent 602 for supply to absorber 504. Filter 656 is configured to filter and / or clean lean solvent 602 used in absorber 504. In some embodiments, solvent circuit 510 may include additional components (e.g., heat exchangers, filters, valves, etc.) and / or exclude one or more of the illustrated components. Stripper 506 is used to process gas-rich solvent 620, as discussed below.

[0083] Stripper 506 includes multiple stripper sections 658 disposed within a container or housing 660, wherein housing 660 includes a solvent inlet 662, a solvent outlet 664, and a gas outlet 666. Housing 660 has a top portion 668, a bottom portion 670, and an intermediate portion 672 axially disposed between the top portion 668 and the bottom portion 670 relative to a central axis 674 of housing 660. Top portion 668 includes a top plate or cover 676 having a gas outlet 666 coaxial with central axis 674. However, gas outlet 666 may be disposed off-center from central axis 674 or at other locations along top portion 668. Intermediate portion 672 includes sidewalls 678 extending about central axis 674. For example, sidewall 678 may be an annular sidewall, square sidewall, rectangular sidewall, or any other suitable shape extending about central axis 674. In some embodiments, gas outlet 666 may be disposed in sidewall 678 along top portion 668. Additionally, the solvent inlet 662 may be disposed along the top portion 668 or the middle portion 672. The bottom portion 670 may include a substrate 680 below the solvent outlet 664. In the illustrated embodiment, the solvent outlet 664 is disposed in the sidewall 678 along the bottom portion 670. However, in some embodiments, the solvent outlet 664 may be disposed in the substrate 680 within the bottom portion 670.

[0084] The plurality of stripper sections 658 within the internal volume 682 of the housing 660 may include any number and type of stripper sections 658, such as stripper sections 684, 686, 688, 690, and 692. These stripper sections may include packing, support trays or screens, wire mesh, solvent dispensers with nozzles, vapor dispensers with nozzles, or any combination thereof, in any configuration. For example, each packing may include a plurality of beads, balls, or mixture-inducing structures configured to facilitate mixing between a flow of solvent (e.g., rich gas solvent 620) and a flow of vapor 694 in the stripper 506. Each support tray or screen may include wire mesh, a plate with multiple openings, or another suitable structure that holds the packing in place while allowing fluid flow of solvent (e.g., rich gas solvent 620) and vapor 694 through the support tray or screen. Each solvent dispenser may include a plurality of solvent nozzles configured to dispense solvent across the internal volume 682. Each steam distributor may include multiple fluid nozzles configured to distribute steam 694 across an internal volume 682. In some embodiments, stripper sections 686, 688, and 692 include wire mesh, stripper section 684 includes packing and a support tray or screen, and stripper section 690 includes a baffle or partition plate with one or more openings. However, stripper sections 658 (e.g., 684, 686, 688, 690, and 692) are not limited to the illustrated configurations.

[0085] As discussed above, stripper 506 is configured to strip unwanted gases from gas-rich solvent 620 using heated fluid 502 supplied via heated fluid loop 512 from one or more of the following: WHR system 22 (e.g., thermodynamic cycle 24 and / or heat storage system 140), steam turbine system 14, steam generation system 16, another waste heat recovery system of combined cycle system 10, or combinations thereof. In the illustrated embodiments, heated fluid loop 512 is coupled to various heated fluid extraction locations 530 and heated fluid injection locations 532 (e.g., 540, 542, 544, and 546) to provide heat in the form of heated fluid 502 for supporting stripper 506. Each of these heated fluid loops 512 may be configured to transfer heat to the solvent in stripper 506 via direct heat transfer (e.g., direct injection into the solvent), indirect heat transfer (e.g., via a heat exchanger), or any combination thereof. Controller 220 is configured to selectively control (e.g., open and close) valve 534 to control the corresponding flow of heated fluid 502 through heated fluid circuit 512 to stripper 506. In an illustrated embodiment, heated fluid circuit 512 includes heated fluid circuits (or circuit portions) 696, 698, 700, and 702 coupled to corresponding heated fluid injection positions 532 (e.g., 540, 542, 544, and 546). For example, heated fluid circuits 512 (e.g., 698 and 700) are coupled to the intermediate portion 672 of housing 660 at corresponding heated fluid injection positions 532 (e.g., 542 and 544) located between stripper sections 686 and 688. However, heated fluid circuits 698 and 700 may be coupled to stripper 506 at any suitable heated fluid injection position 532, which may be the same or different between heated fluid circuits 698 and 700. For example, heated fluid injection locations 532 (e.g., 542 and 544) may be located directly at, above, and / or below one or more stripper sections in stripper section 658. Additionally, heated fluid injection locations 532 (e.g., 542 and 544) may include a fluid distributor having a plurality of fluid nozzles configured to distribute heated fluid 502 across the internal volume 682 of stripper 506.

[0086] In the illustrated embodiments, stripper 506 may be coupled to or include one or more additional components, such as thermal control system 706 and moisture removal system 708. Thermal control system 706 may be coupled to any part of stripper 506, such as at bottom portion 670. Thermal control system 706 may include solvent recirculation loop 710 with reboiler 712 configured to heat and boil solvent for recirculation into stripper 506. In the illustrated embodiments, reboiler 712 is coupled to at least one heated fluid loop (e.g., 696) in heated fluid loop 512 as a heat source for heating and boiling solvent, rather than relying on a separate or independent heat source. However, in some embodiments, reboiler 712 may include one or more additional heat sources for heating solvent, such as electric heaters, burners or furnaces, steam generators, or other heat sources. Additional heat sources may be used when steam is unavailable and / or insufficient to provide the desired heating in reboiler 712.

[0087] However, in the illustrated embodiment, the heated fluid loop 512 may be the primary heat source supporting the reboiler 712. For example, at least one heated fluid loop (e.g., 696) in the heated fluid loop 512 supplies heated fluid 502 to the reboiler 712 at an inlet 714 (e.g., heated fluid injection location 540), while the reboiler 712 discharges water and / or steam at an outlet 716. The discharged water and / or steam flows from the reboiler 712 to the heated fluid source 528 (e.g., WHR system 22, including thermodynamic cycle 24 and / or heat storage system 140) via a return loop 718, wherein the return loop 718 may include a fluid handling unit (FTU) 720 configured to treat the heated fluid 502 before returning to the heated fluid source 528. For example, the FTU 720 may include a condenser, particulate filter, descaling unit, ultraviolet (UV) treatment unit, or any combination thereof configured to condense steam and / or other liquid vapors into condensate. In the illustrated embodiment, return loop 718 is coupled to pump 722, which is configured to pump heated fluid 502 back to heated fluid source 528. Although heated fluid loop 512 (e.g., 696) is coupled to reboiler 712, any one or more heated fluid loops in heated fluid loop 512 (e.g., 696, 698, 700, and 702) may be coupled to reboiler 712 to provide heated fluid 502 as a heat source for heating and boiling the solvent in stripper 506.

[0088] In some embodiments, at least one of the heated fluid loops (e.g., 702) in the heated fluid loop 512 supplies heated fluid 502 to a heated fluid injection position 544 at a heat exchanger 704 disposed along the solvent loop 510, thereby heating the rich gaseous solvent 620 between the absorber 504 and the stripper 506. For example, the heat exchanger 704 may be disposed between the heat exchanger 650 and the solvent inlet 662 leading into the stripper 506. In some embodiments, the heated fluid 502 may be injected directly into the rich gaseous solvent 620, such that the heated fluid 502 mixes with the rich gaseous solvent 602 and heat is directly transferred to the rich gaseous solvent. However, in some embodiments, the heat exchanger 704 provides indirect heat transfer between the heated fluid 502 and the rich gaseous solvent 602, and thus the heated fluid 502 may be recirculated back to the heated fluid source 528 along a return loop (e.g., return loop 718).

[0089] The moisture removal system 708 may include a condenser loop 724 having a condenser 726, wherein the condenser loop 724 is coupled to a gas outlet 666 and a return inlet 728. The condenser 726 is configured to cool and condense any vapors and solvent vapors present in the captured gas 204 discharged from the stripper 506, thereby outputting water or condensate 730, captured gas 204 substantially free of water content and solvent vapors, and solvent vapors for return to the stripper 506 via the return inlet 728. In some embodiments, the condenser 726 includes a heat exchanger (e.g., a 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 housing 660. However, the moisture removal system 708 may be located at any suitable location to condense any vapors and solvent vapors present in the captured gas 204. The captured gas 204 may also be compressed in a compression system 206 and delivered to a storage device and / or line 208 as discussed above.

[0090] In operation, controller 220 is configured to monitor sensor 222 and control the operation of solvent-based gas capture system 500 to support stripper 506 using heated fluid 502 supplied via heated fluid loop 512. For example, controller 220 may selectively control valve 534 depending on the following: the condition of heated fluid 502 supplied via one or more of the heated fluid loops 512; the temperature of the solvent in stripper 506; the temperature of the solvent in reboiler 712; the operating conditions of combined circulation system 10 (e.g., start-up mode, steady-state mode, shutdown mode, full-load mode, and / or partial-load mode); the percentage of undesired gases in air 190 and / or other gases; the flow rate of lean solvent 602; the flow rate of rich solvent 620; the flow rate of gas 600; or any combination thereof. During start-up, shutdown, and / or partial load modes, if the heated fluid 502 is unavailable or limited, controller 220 may be configured to control one or more additional heat sources (e.g., electric heaters, furnaces, etc.) and / or heat storage system 140 to provide heat to support stripper 506. During steady-state mode, if the heated fluid 502 is available, controller 220 may be configured to control WHR system 22 (e.g., thermodynamic cycle 24 and / or heat storage system 140), steam turbine system 14, steam generation system 16, valve 534, or any combination thereof to supply heated fluid 502 to stripper 506. In some embodiments, controller 220 may be configured to control the mixing of heated fluid 502 from various heated fluid extraction locations 530 to provide heated fluid 502 at the desired temperature and pressure to support stripper 506. However, the solvent-based gas capture system 500 can be configured to selectively use a heated fluid 502 from the WHR system 22 (e.g., thermodynamic cycle 24 and / or thermal storage system 140), steam turbine system 14, steam generation system 16, or any combination thereof. Depending on the heated fluid source 528 and the type of heat transfer (e.g., direct or indirect heat transfer), the heated fluid 502 may include heated water, steam, a solvent (e.g., the same solvent used in the solvent-based gas capture system 500), a supercritical fluid (e.g., the same or different supercritical fluid used in the thermodynamic cycle 24), or any combination thereof.

[0091] Figure 4 yes Figure 1A schematic diagram of an embodiment of the combined circulation system 10 illustrates a heat source 26 of a power generation system 12 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) connected along a flow path 750 of the thermal fluid 30 (e.g., along fluid loop 110) to the thermodynamic cycle 24 of the WHR system 22, wherein the thermodynamic cycle 24 and / or thermal storage system 140 are configured to provide thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18. As discussed above, the gas capture system 20 may include an adsorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or any combination thereof. For example, the gas capture system 20 may include... Figure 2 250 and / or adsorbent-based gas capture systems Figure 3 The solvent-based gas capture system 500. Various aspects of the combined cycle system 10, such as the power generation system 12, steam turbine system 14, steam generation system 16, DAC system 18, and gas capture system 20 and WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140), may be substantially the same as those discussed above. However, Figure 4 Examples can be found Figures 1 to 3 Additional details of the thermodynamic cycle 24 of the WHR system 22 used.

[0092] In the illustrated embodiment, the thermodynamic cycle 24 includes a fluid loop or circuit 752 that intersects the flow path 750 at the main heat exchanger 754 of the WHR system 22. The main heat exchanger 754 is configured to exchange heat from the hot fluid 30 along the flow path 750 to the working fluid 756 (e.g., working fluid 32) in the fluid loop 752, thereby recovering waste heat from the hot fluid 30 to heat the working fluid 756 in the thermodynamic cycle 24. As discussed above, the working fluid 756 may include one or more supercritical fluids (SCFs), inert gases (such as rare gases), organic working fluids, or any combination thereof. For example, an SCF may include supercritical carbon dioxide (sCO2) or a blend of sCO2 with one or more dopants. By another example, a rare gas may include helium (He), xenon (Xe), or a combination thereof (e.g., a He-Xe mixture). By another example, an inert gas may include nitrogen. By further examples, the organic working fluid may include hydrocarbons (HCs), perfluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof. In an illustrated embodiment, the working fluid 756 may include an SCF, such as sCO2 or a blend of sCO2 having one or more dopants. Dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants. In some embodiments, the sCO2 blend may have 5% mol to 20% mol of dopants to increase the supercritical temperature of sCO2. For example, the dopants may increase the critical temperature of sCO2 to about 70°C to 100°C without a significant decrease in efficiency. Therefore, the amount of waste heat can be increased by condensing the sCO2 blend at a higher temperature. Thus, all or substantially all of the waste heat discharged from thermodynamic cycle 24 can be used as heat fluid 34 for the DAC system 18. If the heat exceeds the heat requirements of the DAC system 18, the excess heat can be stored in the heat storage system 140, as discussed in detail above.

[0093] Thermodynamic cycle 24 has multiple components 751, including, for example, a compressor 758, a regenerator 760, a main heat exchanger 754, a turbine 762, a waste heat recovery (WHR) heat exchanger 764, and a precooler 766 arranged along a fluid loop 752. The fluid loop 752 includes multiple fluid lines or conduits 768, 770, 772, 774, 776, 778, and 780, and internal flow paths through the multiple components 751. Components 751 may also include multiple valves and sensors disposed at each component, upstream and / or downstream of the component 751, wherein a controller 220 is communicatively coupled to the valves, sensors, and components 751 to control the thermodynamic cycle 24. In the illustrated embodiment, the working fluid 756 passes through the fluid loop 752, sequentially through the compressor 758, fluid conduit 768, regenerator 760, fluid conduit 770, main heat exchanger 754, fluid conduit 772, turbine 762, fluid conduit 774, regenerator 760, fluid conduit 776, WHR heat exchanger 764, fluid conduit 778, precooler 766, and fluid conduit 780, before returning to the compressor 758. As discussed above, the main heat exchanger 754 recovers heat from the hot fluid 30 to heat the working fluid 756. Conversely, the WHR heat exchanger 764 discharges waste heat from the working fluid 756 (i.e., heat that would otherwise be discharged into the precooler 766) as a heat source to supply the hot fluid 34 from the thermodynamic cycle 24 to the gas capture system 20 of the DAC system 18.

[0094] In operation, compressor 758 is configured to compress working fluid 756 (e.g., SCF) and supply the compressed working fluid 756 along fluid conduit 768 to regenerator 760. Compressor 758 may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft driven to rotate by turbine 762 via shaft 782. Regenerator 760 includes a heat exchanger having a first internal flow path 784 between fluid conduits 774 and 776 and a second internal flow path 786 between fluid conduits 768 and 770, wherein regenerator 760 is configured to transfer heat from working fluid 756 in the second internal flow path 786 to working fluid 756 in the first internal flow path 784. Therefore, the regenerator 760 increases the temperature of the working fluid 756 (e.g., the heated working fluid) supplied to the main heat exchanger 754 via the fluid conduit 776, and decreases the temperature of the working fluid 756 (e.g., the cooled working fluid) supplied to the WHR heat exchanger 764 via the fluid conduit 770. For example, the temperature of the cooled working fluid 756 may be approximately 100 to 150 degrees Celsius, 100 to 140 degrees Celsius, or 100 to 130 degrees Celsius.

[0095] The main heat exchanger 754 of thermodynamic cycle 24 includes a first internal flow path 788 between fluid conduits 770 and 772 of fluid loop 752 and a second internal flow path 790 between fluid conduits 792 and 794 of flow path 750, wherein the main heat exchanger 754 is configured to transfer heat from hot fluid 30 in the second internal flow path 790 to working fluid 756 in the first internal flow path 788. Therefore, the main heat exchanger 754 increases the temperature of the working fluid 756 (e.g., heated working fluid) supplied to turbine 762 through fluid conduit 794 and decreases the temperature of the hot fluid 30 (e.g., cooled hot fluid) discharged through fluid conduit 772. In some embodiments, the main heat exchanger 754 may be configured to increase the temperature of the working fluid 756 to approximately 550°C to 700°C, or at least equal to or greater than approximately 500°C, 510°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, or 650°C. The heated working fluid 756 then expands via the turbine 762, as discussed in further detail below.

[0096] In some embodiments, the main heat exchanger 754 may receive hot fluid 30 (e.g., hot or heated hot fluid) at a temperature of approximately 570°C to 720°C and output hot fluid 30 (e.g., cold or cooled hot fluid) at a temperature range of approximately 50°C to 100°C (such as approximately 50°C, 60°C, 70°C, 80°C, 90°C, or 100°C plus or minus 1°C, 2°C, 3°C, 4°C, or 5°C). The hot fluid 30 then passes through a heat source 26 for reheating by one or more thermal power generation systems in the thermal power generation system 28 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54).

[0097] In fluid loop 752, turbine 762 receives heated working fluid 756 from main heat exchanger 754. Turbine 762 may include one or more turbines and / or turbine stages. The heated working fluid 756 expands through turbine 762, thereby driving the rotation of turbine blades and turbine shaft of turbine 762 to drive the rotation of shaft 782 coupled to compressor 758. Turbine 762 may also be coupled to load 798, such as a mechanical load and / or generator. In some embodiments, load 798 is the primary function of thermodynamic cycle 24, causing thermodynamic cycle 24 to use heat from heat source 26 to generate mechanical force and / or electricity. As working fluid 756 expands through turbine 762, the temperature of working fluid 756 decreases, and the pressure upstream of regenerator 760 decreases. However, working fluid 756 still contains excess heat.

[0098] The working fluid 756 from turbine 762 then flows through regenerator 760, which cools the working fluid 756 upstream of WHR heat exchanger 764 (e.g., cooling the working fluid), as discussed above. For example, the temperature of the cooled working fluid 756 upon reaching WHR heat exchanger 764 can 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. WHR heat exchanger 764 is configured to extract or discharge waste heat from working fluid 756 to generate hot fluid 34, which is supplied to one or more gas capture systems 20 of DAC system 18 via one or more fluid loops 800 (e.g., fluid loop 130). Without WHR heat exchanger 764, thermodynamic cycle 24 can discharge waste heat to the environment, rendering the waste heat unused for any useful purpose. Each fluid loop in fluid loop 800 may include a closed-loop fluid loop between the WHR heat exchanger 764 and a gas capture system in the gas capture system 20, wherein fluid loop 800 may include fluid conduits, valves, sensors, flow regulators, and other flow control devices to control the flow of hot fluid 34 via controller 220. One or more fluid loops 800 (e.g., fluid loop 130) are also coupled to heat storage system 140 via fluid loop 150, as discussed in detail above.

[0099] The WHR heat exchanger 764 includes a first internal flow path 802 between fluid conduits 776 and 778 of the fluid circuit 752 and a second internal flow path 804 coupled to the fluid circuit 800 of one or more gas trapping systems 20. The WHR heat exchanger 764 is configured to transfer heat from the working fluid 756 in the first internal flow path 802 to the hot fluid 34 in the second internal flow path 804. Therefore, the WHR heat exchanger 764 increases the temperature of the hot fluid 34 supplied to the gas trapping system 20 through the fluid circuit 800 and decreases the temperature of the working fluid 756 (e.g., cooled working fluid) supplied to the precooler 766 through the fluid conduit 778. In some embodiments, the WHR heat exchanger 764 may be configured to increase the temperature of the hot fluid 34 to 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 can be configured to reduce the temperature of the working fluid 756 to approximately 50 degrees Celsius (e.g., by adding or subtracting 1, 2, 3, 4, or 5 degrees Celsius), or between approximately 40 and 60 degrees Celsius.

[0100] The precooler 766 may include one or more heat exchangers configured to transfer heat from the working fluid 756 to the environment via a suitable cooling fluid (e.g., river water or ambient air), thereby reducing the temperature of the working fluid 756 upstream of the compressor 758. For example, the precooler 766 may be configured to reduce the temperature of the working fluid 756 to approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or between 30 and 50 degrees Celsius, or between 40 and 50 degrees Celsius. The working fluid 756 then returns to the compressor 758 to pass through the fluid loop 752 of the thermodynamic cycle 24 again.

[0101] In the illustrated embodiments, the main heat exchanger 754 extracts waste heat from the hot fluid 30 to help drive the thermodynamic cycle 24, while the WHR heat exchanger 764 discharges or extracts waste heat from the working fluid 756 (e.g., SCF) to heat the hot fluid 34, thereby helping to drive desorption (or other processes) in the gas capture system 20. In some embodiments, the WHR heat exchanger 764 indirectly transfers heat from the working fluid 756 to the hot fluid 34, such that fluids 34 and 756 are separated from each other. Therefore, fluids 34 and 756 may be the same or different from each other. The hot fluid 34 may include, for example, water, steam, SCF, a solvent (e.g., a solvent used in a solvent-based gas capture system), or any other suitable heat transfer fluid. In some embodiments, the WHR heat exchanger 764 may be configured to transfer or circulate a portion of the working fluid 756 through a fluid loop 800 between the thermodynamic cycle 24 and the gas capture system 20. However, 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 system 20.

[0102] As discussed above, the DAC system 18 includes one or more gas capture systems 20 configured to process air 190 and / or other gases. Air 190 is compressed by one or more compressors 210, such that the gas capture system 20 receives the compressed air 190 for processing. The DAC system 18 is configured to capture unwanted gases (e.g., CO2) from the air 190 and then output treated air 191 and captured gas 204. The treated air 191 typically has a concentration of unwanted gases (e.g., CO2) substantially below atmospheric levels. A heat fluid 34 at least supports (e.g., as a heat source) the desorption mode in the gas capture system 20. Depending on the heat demand in the gas capture system 20, the heat fluid 34 may be supplied to the DAC system 18 from the thermodynamic cycle 24 and / or the heat storage system 140. If excess heat cannot be used in the DAC system 18 and / or the heat storage system 140, the excess heat may be discharged to the atmosphere via the heat exchanger 162 of the waste heat discharge system 160.

[0103] Figure 5 yes Figure 1A schematic diagram of an embodiment of the combined circulation system 10 illustrates a heat source 26 of a power generation system 12 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) connected along a flow path 850 of the thermal fluid 30 (e.g., along fluid loop 110) to the thermodynamic cycle 24 of the WHR system 22, wherein the thermodynamic cycle 24 and / or thermal storage system 140 are configured to provide thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18. As discussed above, the gas capture system 20 may include an adsorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or any combination thereof. For example, the gas capture system 20 may include... Figure 2 250 and / or adsorbent-based gas capture systems Figure 3 The solvent-based gas capture system 500. Various aspects of the combined cycle system 10, such as the power generation system 12, steam turbine system 14, steam generation system 16, DAC system 18, and gas capture system 20 and WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140), may be substantially the same as those discussed above. However, Figure 5 Examples can be found Figures 1 to 3 Additional details of the thermodynamic cycle 24 of the WHR system 22 used.

[0104] In the illustrated embodiment, the thermodynamic cycle 24 includes a fluid loop or circuit 852 that intersects the flow path 850 at a plurality of main heat exchangers 854 of the WHR system 22. Each main heat exchanger 854 is configured to exchange heat from the hot fluid 30 along the flow path 850 to the working fluid 856 (e.g., working fluid 32) in the fluid loop 852, thereby transferring heat from the hot fluid 30 to heat the working fluid 856 in the thermodynamic cycle 24. As discussed above, the working fluid 856 may include one or more supercritical fluids (SCFs), inert gases (such as rare gases), organic working fluids, or any combination thereof. For example, an SCF may include supercritical carbon dioxide (sCO2) or a blend of sCO2 with one or more dopants. By another example, a rare gas may include helium (He), xenon (Xe), or a combination thereof (e.g., a He-Xe mixture). By another example, an inert gas may include nitrogen. By further examples, the organic working fluid may include hydrocarbons (HCs), perfluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof. In an illustrated embodiment, the working fluid 856 may include an SCF, such as sCO2 or a blend of sCO2 having one or more dopants. Dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants. In some embodiments, the sCO2 blend may have 5% mol to 20% mol of dopants to increase the supercritical temperature of sCO2. For example, the dopants may increase the critical temperature of sCO2 to about 70°C to 100°C without a significant decrease in efficiency. Therefore, the amount of waste heat can be increased by condensing the sCO2 blend at a higher temperature. Thus, all or substantially all of the waste heat discharged from thermodynamic cycle 24 can be used as heat fluid 34 for the DAC system 18. If the heat exceeds the heat demand of the DAC system 18, the excess heat can be stored in the heat storage system 140, as discussed in detail above. The WHR system 22 may include any number of main heat exchangers 854, such as 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more main heat exchangers 854. In the illustrated embodiment, the main heat exchangers 854 include main heat exchangers 858 and 860.

[0105] Thermodynamic cycle 24 has multiple components 862, including, for example, one, two, or more compressors 864, a waste heat recovery (WHR) heat exchanger 866, a main heat exchanger 854, a regenerator 868 (e.g., a heat exchanger), a turbine 870, and a precooler 872 arranged along a fluid loop 852, wherein the fluid loop 852 includes multiple fluid lines or conduits 874 fluidly connecting the components to the components. Components 862 may also include multiple valves and sensors disposed at each component, upstream and / or downstream, wherein a controller 220 is communicatively coupled to the valves, sensors, and components 862 to control the thermodynamic cycle 24. In an illustrated embodiment, one or more compressors 864 include compressor 876, WHR heat exchanger 866 includes WHR heat exchanger 878, regenerator 868 includes regenerator 880, turbine 870 includes turbines 882 and 884, and precooler 872 includes precooler 886. Figure 5 Thermodynamic cycle 24 operates substantially the same as the plurality of main heat exchangers 854 (e.g., main heat exchangers 858 and 860) and the plurality of turbines 870 (e.g., turbines 882 and 884) discussed above. As discussed above, the main heat exchangers 854 (e.g., main heat exchangers 858 and 860) recover heat from the hot fluid 30 to heat the working fluid 856, wherein heat source 26 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) provides heat for heating the hot fluid 30 and generating electricity in the turbines 870. Additionally, a WHR heat exchanger 866 (e.g., WHR heat exchanger 878) discharges waste heat from the working fluid 856 as a heat source to supply the hot fluid 34 from thermodynamic cycle 24 to the gas capture system 20 of DAC system 18.

[0106] In the illustrated embodiment, component 862 of thermodynamic cycle 24 is arranged downstream of compressor 864 (e.g., compressor 876) and upstream of turbine 870 (e.g., turbines 882 and 884) along a relatively high-pressure (HP) loop portion 888 of fluid loop 852, or downstream of turbine 870 (e.g., turbines 882 and 884) and upstream of compressor 864 (e.g., compressor 876) along a relatively low-pressure (LP) loop portion 890 of fluid loop 852. Compressor 864 (e.g., compressor 876) transitions from LP loop portion 890 to HP loop portion 888 of fluid loop 852 by compressing working fluid 856. Turbines 870 (e.g., turbines 882 and 884) transition from the HP loop portion 888 to the LP loop portion 890 of 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 generators) and shafts (e.g., shafts coupled to compressor 864). In some embodiments, loads 883 and 885 are the primary function of thermodynamic cycle 24, such that thermodynamic cycle 24 uses heat from heat source 26 to generate mechanical force and / or electricity. In an illustrated embodiment, main heat exchangers 858 and 860 are disposed along and fluidly coupled to fluid circuit 852 upstream of the respective turbines 882 and 884, such that main heat exchanger 858 is along HP loop portion 888, and main heat exchanger 860 is located at the transition between HP loop portion 888 and LP loop portion 890 of fluid circuit 852. A regenerator 880 is located at the intersection 892 between the HP loop section 888 and the LP loop section 890 of the fluid loop 852. A WHR heat exchanger 866 (e.g., a WHR heat exchanger 878) and a precooler 872 (e.g., a precooler 886) are disposed along and fluidly connected to the LP loop section 890 of the fluid loop 852.

[0107] In operation, compressor 864 (e.g., compressor 876) is configured to compress working fluid 856 (e.g., working fluid 32) and supply the compressed working fluid 856 to regenerator 892 (e.g., regenerator 880). Compressor 864 (e.g., compressor 876) may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft driven to rotate via one or more shafts by one or more turbines 870 (e.g., turbines 882 and 884). Regenerator 880 transfers heat between working fluid 856 along HP loop section 888 (e.g., between compressor 864 and turbine 870) and LP loop section 890 (e.g., between turbine 870 and compressor 864), thereby heating working fluid 856 upstream of turbine 870 and cooling working fluid 856 upstream of WHR heat exchanger 866. Working fluid 856 continues to flow along HP loop section 890 from regenerator 880 to main heat exchanger 858.

[0108] As discussed above, the main heat exchangers 854 (e.g., main heat exchangers 858 and 860) are configured to use heat from 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 hot fluid 30. The main heat exchanger 858 transfers heat from the hot fluid 30 along flow path 850 (e.g., fluid loop 110) to the working fluid 856 along fluid loop 852, thereby heating the working fluid 856 before turbine 882. Turbine 882 is driven and expanded by the heated working fluid 856 from the main heat exchanger 860, and outputs the working fluid 856 at a relatively low pressure to the next main heat exchanger 858. Similarly, the main heat exchanger 860 transfers heat from the hot fluid 30 along flow path 850 (e.g., fluid loop 110) to the working fluid 856 along fluid loop 852, thereby heating the working fluid 856 before turbine 884. Turbine 884 is driven and expanded by heated working fluid 856 from main heat exchanger 860, and outputs working fluid 856 at a relatively low pressure to be delivered along LP loop section 890 to regenerator 880 at crossover point 892. In some embodiments, thermodynamic cycle 24 may include any number of pairs of main heat exchangers 854 and turbines 870 (e.g., 1, 2, 3, 4, 5 or more), wherein each pair includes at least one main heat exchanger in the corresponding turbine upstream of one of the main heat exchangers 854 in turbine 870. As discussed above, regenerator 880 transfers heat between working fluid 856 along HP loop section 888 and LP loop section 890, thereby cooling working fluid 856 before WHR heat exchanger 866 (e.g., WHR heat exchanger 878).

[0109] The WHR heat exchanger 878 is configured to transfer heat to cool the working fluid 856 (e.g., cooled working fluid) along the LP loop portion 890 between the regenerator 880 and the precooler 886, while simultaneously heating the working fluid (e.g., hot fluid 34) along the fluid loop 130 coupled to one or more gas trapping systems 20 of the DAC system 18. In some embodiments, the WHR heat exchanger 878 may be configured to increase the temperature of the hot fluid 34 to 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. Additionally, the WHR heat exchanger 878 can be configured to reduce the temperature of the working fluid 856 to approximately 50 degrees Celsius (e.g., by adding or subtracting 1, 2, 3, 4, or 5 degrees Celsius), or between approximately 40 and 60 degrees Celsius.

[0110] Downstream of the WHR heat exchanger 878, in the LP loop section 890, a precooler 872 (e.g., precooler 886) 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 the temperature of the working fluid 856 upstream of the compressor 864 (e.g., compressor 876). For example, the precooler 872 (e.g., precooler 886) may be configured to reduce the temperature of the working fluid 856 to approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or between 30 and 50 degrees Celsius or between 40 and 50 degrees Celsius. The working fluid 856 then returns to the compressor 864 (e.g., compressor 876) to pass through the fluid loop 852 of the thermodynamic cycle 24 again.

[0111] As the cycle repeats in thermodynamic cycle 24, heat source 26 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) provides heat to drive turbine 870 via heat exchange in main heat exchangers 854 (e.g., main heat exchangers 858 and 860), while DAC system 18 (e.g., gas capture system 20) uses waste heat extracted from thermodynamic cycle 24 via WHR heat exchanger 866 (e.g., WHR heat exchanger 878). WHR heat exchanger 878 is configured to extract or discharge waste heat from working fluid 856 to generate hot fluid 34, which is supplied to one or more gas capture systems 20 of DAC system 18 via fluid loop 130. Without WHR heat exchanger 878, thermodynamic cycle 24 can discharge waste heat to the environment, rendering the waste heat unused for any useful purpose. Hot fluid 34 can transfer heat to gas capture system 20 during desorption mode, thereby facilitating the desorption of undesirable gases (e.g., CO2) from air 190 or other gases. If the heat fluid 34 contains excess heat beyond the needs of the DAC system 18, the heat storage system 140 stores the excess heat for later use by the DAC system 18. For example, if the heat fluid 34 contains insufficient heat to support the needs of the DAC system 18, the heat storage system 140 may supply the heat fluid 34 to the DAC system 18.

[0112] Figure 6 yes Figure 1 A schematic diagram of an embodiment of the combined circulation system 10 illustrates a heat source 26 of a power generation system 12 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) connected along a flow path 910 of the thermal fluid 30 (e.g., along fluid loop 110) to the thermodynamic cycle 24 of the WHR system 22, wherein the thermodynamic cycle 24 and / or heat storage system 140 are configured to provide thermal fluid 34 to one or more gas capture systems 20 of the DAC system 18. As discussed above, the gas capture system 20 may include an adsorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or any combination thereof. For example, the gas capture system 20 may include... Figure 2 250 and / or adsorbent-based gas capture systems Figure 3 The solvent-based gas capture system 500. Various aspects of the combined cycle system 10, such as the power generation system 12, steam turbine system 14, steam generation system 16, DAC system 18, and gas capture system 20 and WHR system 22 (e.g., thermodynamic cycle 24 and thermal storage system 140), may be substantially the same as those discussed above. However, Figure 6 Examples can be found Figures 1 to 3 Additional details of the thermodynamic cycle 24 of the WHR system 22 used.

[0113] In the illustrated embodiment, the thermodynamic cycle 24 includes a fluid loop or circuit 912 that intersects the flow path 910 at a plurality of main heat exchangers 914 of the WHR system 22. Each main heat exchanger 914 is configured to exchange heat from the hot fluid 30 along the flow path 910 to the working fluid 916 (e.g., working fluid 32) in the fluid loop 912, thereby recovering heat from the hot fluid 30 to heat the working fluid 916 in the thermodynamic cycle 24. As discussed above, the working fluid 916 may include one or more supercritical fluids (SCFs), inert gases (such as rare gases), organic working fluids, or any combination thereof. For example, an SCF may include supercritical carbon dioxide (sCO2) or a blend of sCO2 with one or more dopants. By another example, a rare gas may include helium (He), xenon (Xe), or a combination thereof (e.g., a He-Xe mixture). By another example, an inert gas may include nitrogen. By further examples, the organic working fluid may include hydrocarbons (HCs), perfluorocarbons (PFCs), hydrofluorocarbons (HFCs), siloxanes, and inorganic substances, or any combination thereof. In an illustrated embodiment, the working fluid 916 may include an SCF, such as sCO2 or a blend of sCO2 having one or more dopants. Dopants may include, for example, sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants. In some embodiments, the sCO2 blend may have 5% mol to 20% mol of dopants to increase the supercritical temperature of sCO2. For example, the dopants may increase the critical temperature of sCO2 to about 70°C to 100°C without a significant decrease in efficiency. Therefore, the amount of waste heat can be increased by condensing the sCO2 blend at a higher temperature. Thus, all or substantially all of the waste heat discharged from thermodynamic cycle 24 can be used as heat fluid 34 for the DAC system 18. If the heat exceeds the heat demand of the DAC system 18, the excess heat can be stored in the heat storage system 140, as discussed in detail above. The WHR system 22 may include any number of main heat exchangers 914, such as 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more main heat exchangers 914. In the illustrated embodiment, the main heat exchangers 914 include main heat exchangers 918 and 920.

[0114] Thermodynamic cycle 24 has multiple components 922, including, for example, one, two or more compressors 924, a waste heat recovery (WHR) heat exchanger 926, a main heat exchanger 914, a regenerator 928 (e.g., a heat exchanger), a turbine 930, and a precooler 932 arranged along a fluid loop 912, wherein the fluid loop 912 includes multiple fluid lines or conduits 934 fluidly connecting the components between them. Components 922 may also include multiple valves and sensors disposed upstream and / or downstream of each component in the component 922, wherein a controller 220 is communicatively coupled to the valves, sensors, and components 922 to control the thermodynamic cycle 24. In an illustrated embodiment, one or more compressors 924 include compressors 936 and 938, the WHR heat exchanger 926 includes a WHR heat exchanger 940, the regenerator 928 includes regenerators 942 and 944, the turbine 930 includes turbines 946 and 948, and the precooler 932 includes a precooler 950. Component 922 also includes a mixer 952 and a splitter 954. Figure 6 The thermodynamic cycle 24 operates substantially the same as the plurality of compressors 924 (e.g., compressors 936 and 938), plurality of regenerators 928 (e.g., regenerators 942 and 944), plurality of main heat exchangers 914 (e.g., main heat exchangers 918 and 920), and plurality of turbines 930 (e.g., turbines 946 and 948) discussed above. As discussed above, the main heat exchangers 914 (e.g., main heat exchangers 918 and 920) recover heat from the hot 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 hot fluid 30. Additionally, the WHR heat exchanger 926 (e.g., WHR heat exchanger 940) discharges waste heat from the working fluid 916 as a heat source to supply the hot fluid 34 from the thermodynamic cycle 24 to the gas capture system 20 of the DAC system 18.

[0115] In the illustrated embodiment, a component 922 of the thermodynamic cycle 24 is arranged downstream of the compressor 924 (e.g., compressors 936 and 938) and upstream of the turbine 930 (e.g., turbines 946 and 948) along a relatively high-pressure (HP) circuit portion 956 of the fluid circuit 912, or downstream of the turbine 930 (e.g., turbines 946 and 948) and upstream of the compressor 924 (e.g., compressors 936 and 938) along a relatively low-pressure (LP) circuit portion 958 of the fluid circuit 912. The compressor 924 (e.g., compressors 936 and 938) transitions from the LP circuit portion 958 to the HP circuit portion 956 of the fluid circuit 912 by compressing the working fluid 916. Turbines 930 (e.g., turbines 946 and 948) transition from the HP loop portion 956 to the LP loop 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 generators) and shafts (e.g., shafts coupled to compressor 924). In some embodiments, loads 947 and 949 are the primary function of the thermodynamic cycle 24, such that the thermodynamic cycle 24 uses heat from heat source 26 to generate mechanical force and / or electricity. In an illustrated embodiment, main heat exchangers 918 and 920 are disposed along and fluidly coupled to the fluid circuit 912 upstream of the respective turbines 946 and 948, such that main heat exchanger 918 is along the HP loop portion 956, and main heat exchanger 920 is located at the transition between the HP loop portion 956 and the LP loop portion 958 of the fluid circuit 912. Regenerators 942 and 944 are located at corresponding intersections 960 and 962 between the HP loop section 956 and the LP loop section 958 of the fluid loop 912. A WHR heat exchanger 926 (e.g., WHR heat exchanger 940) and a precooler 932 (e.g., precooler 950) are disposed along and fluidly connected to the LP loop section 958 of the fluid loop 912.

[0116] In operation, compressor 924 (e.g., compressors 936 and 938) is configured to compress working fluid 916 (e.g., working fluid 32) and supply the compressed working fluid 916 to HP loop section 956. Compressor 924 (e.g., compressors 936 and 938) may include one or more compressors or compressor stages having compressor blades coupled to a compressor shaft driven to rotate via one or more shafts by one or more turbines 930 (e.g., turbines 946 and 948). In the illustrated embodiment, compressor 936 supplies the compressed working fluid 916 to regenerator 942 at intersection 960. Regenerator 942 transfers heat between the working fluid 916 along the HP loop section 956 (e.g., between compressor 938 and mixer 952) and the LP loop section 958 (e.g., between regenerator 944 and splitter 954), thereby heating the working fluid 916 upstream of mixer 952 and turbine 930 along the HP loop section 956 and cooling the working fluid 916 upstream of splitter 954 (and compressor 936 and WHR heat exchanger 940) along the LP loop section 958. Compressed working fluid 916 from compressor 936 continues to flow through HP loop section 956 to mixer 952. Additionally, compressor 938 supplies compressed working fluid 916 to mixer 952, such that the compressed working fluid 916 from both compressor 936 and 936 is mixed before being delivered to regenerator 944 at intersection 962. Regenerator 944 transfers heat between working fluid 916 along HP loop section 956 (e.g., between mixer 952 and main heat exchanger 918) and LP loop section 958 (e.g., between turbine 948 and regenerator 942), thereby heating working fluid 916 upstream of main heat exchanger 914 and turbine 930 along HP loop section 956 and cooling working fluid 916 upstream of regenerator 942 (and distributor 954 that diverts flow to compressor 938 and WHR heat exchanger 940) along LP loop section 958. Working fluid 916 continues to flow along HP loop section 958 from regenerator 944 to main heat exchanger 918.

[0117] As discussed above, the main heat exchangers 914 (e.g., main heat exchangers 918 and 920) are configured to use heat from 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 hot fluid 30. Main heat exchanger 918 transfers heat from hot fluid 30 along flow path 910 (e.g., fluid loop 110) to working fluid 916 along fluid loop 912, thereby heating working fluid 916 before turbine 946. Turbine 946 is driven and expanded by the heated working fluid 916 from main heat exchanger 920, and outputs working fluid 916 at a relatively low pressure to the next main heat exchanger 918. Similarly, main heat exchanger 920 transfers heat from hot fluid 30 along flow path 910 (e.g., fluid loop 110) to working fluid 916 along fluid loop 912, thereby heating working fluid 916 before turbine 948. Turbine 948 is driven and expanded by heated working fluid 916 from main heat exchanger 920, and outputs working fluid 916 at a relatively low pressure to be delivered along LP loop section 958 to regenerator 944 at crossover point 962, and then to regenerator 942 at crossover point 960. In some embodiments, thermodynamic cycle 24 may include any number of pairs of main heat exchangers 914 and turbines 930 (e.g., 1, 2, 3, 4, 5 or more), wherein each pair includes at least one main heat exchanger of the corresponding turbine upstream of one of the main heat exchangers 914 in turbine 930. As discussed above, regenerators 942 and 944 transfer heat between working fluid 916 along HP loop section 956 and LP loop section 958, thereby cooling working fluid 916 before splitter 954. The distributor 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 exchanger 926 (e.g., WHR heat exchanger 940).

[0118] The WHR heat exchanger 940 is configured to transfer heat to cool the working fluid 916 (e.g., cooled working fluid) along the LP loop portion 958 between the distributor 954 and the precooler 950, while simultaneously heating the working fluid (e.g., hot fluid 34) along the fluid loop 130 coupled to one or more gas trapping systems 20 of the DAC system 18. In some embodiments, the WHR heat exchanger 940 may be configured to increase the temperature of the hot fluid 34 to 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. Additionally, the WHR heat exchanger 940 can be configured to reduce the temperature of the working fluid 916 to approximately 50 degrees Celsius (e.g., by adding or subtracting 1, 2, 3, 4, or 5 degrees Celsius), or between approximately 40 and 60 degrees Celsius.

[0119] Downstream of the WHR heat exchanger 940, in the LP loop section 958, a precooler 932 (e.g., precooler 950) 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 the temperature of the working fluid 916 upstream of the compressor 936. For example, the precooler 932 (e.g., precooler 950) may be configured to reduce the temperature of the working fluid 916 to approximately 40 or 45 degrees Celsius (e.g., plus or minus 1, 2, 3, 4, or 5 degrees Celsius), or between 30 and 50 degrees Celsius, or between 40 and 50 degrees Celsius. The working fluid 916 from the precooler 950 returns to the compressor 936, while the working fluid 916 from the distributor 954 returns to the compressor 938 to again pass through the fluid loop 912 of the thermodynamic cycle 24.

[0120] As the cycle repeats in thermodynamic cycle 24, heat source 26 (e.g., nuclear system 50, combustion system 52, and / or solar thermal system 54) provides heat via heat exchange in main heat exchangers 914 (e.g., main heat exchangers 918 and 920) to drive turbine 930, while DAC system 18 (e.g., gas capture system 20) uses waste heat extracted from thermodynamic cycle 24 via WHR heat exchanger 926 (e.g., WHR heat exchanger 940). WHR heat exchanger 940 is configured to extract or discharge waste heat from working fluid 916 to generate hot fluid 34, which is supplied to one or more gas capture systems 20 of DAC system 18 via fluid loop 130. Without WHR heat exchanger 940, thermodynamic cycle 24 can discharge waste heat to the environment, rendering the waste heat unused for any useful purpose. Hot fluid 34 can transfer heat to gas capture system 20 during desorption mode, thereby facilitating the desorption of undesirable gases (e.g., CO2) from air 190 or other gases. If the heat fluid 34 contains excess heat beyond the needs of the DAC system 18, the heat storage system 140 stores the excess heat for later use by the DAC system 18. For example, if the heat fluid 34 contains insufficient heat to support the needs of the DAC system 18, the heat storage system 140 may supply the heat fluid 34 to the DAC system 18.

[0121] In some implementations, Figures 1 to 6 Various aspects can be combined and used arbitrarily. Therefore, Figures 1 to 6 The embodiments are not intended to be mutually exclusive. Although the illustrated embodiments may be particularly suitable for direct air capture to remove unwanted gases (e.g., CO2) from the air, the illustrated embodiments can be used to capture gases from any gas.

[0122] The disclosed embodiments employ a thermodynamic cycle 24 and / or a thermal storage system 140 to provide hot fluid 34 to one or more gas capture systems 20 of the DAC system 18. Thermodynamic cycle 24 may include one or more separate thermodynamic cycles, one or more loops or sections with heat exchangers and regenerators, or based on... Figures 1 to 6 Any suitable configuration. Thermodynamic cycle 24 is configured to provide heat to an adsorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or any combination thereof. Additionally, the heat source 26 providing heat to thermodynamic cycle 24 may include nuclear system 50, combustion system 52, and / or solar thermal system 54. In some embodiments, only renewable or carbon-free energy may be available for heat source 26. Thus, nuclear system 50 and / or solar thermal system 54 may contribute to providing a carbon-negative power plant.

[0123] As illustrated below, the subject matter described in the detailed description above may be defined by one or more clauses.

[0124] A system includes a direct air capture (DAC) system comprising one or more gas capture systems configured to capture unwanted gases from the air. The system also includes a thermodynamic cycle comprising a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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.

[0125] The system according to the foregoing provisions further includes a heat storage system having one or more heat storage media configured to store heat from the thermodynamic cycle and selectively supply the heat to the one or more gas capture systems.

[0126] According to any of the foregoing provisions, the one or more thermal storage media include sensible thermal energy storage, latent thermal energy storage and / or thermochemical thermal energy storage.

[0127] In any of the foregoing provisions, the system wherein the one or more thermal storage media comprises one or more phase change materials.

[0128] In any of the foregoing provisions, the working fluid in the system comprises supercritical fluid, inert gas, rare gas, organic fluid, or any combination thereof.

[0129] In any of the foregoing provisions, the working fluid in the system comprises a supercritical fluid.

[0130] In any of the foregoing provisions, the supercritical fluid comprises supercritical carbon dioxide (CO2).

[0131] According to any of the foregoing provisions, the supercritical CO2 comprises one or more dopants, and the one or more dopants comprise sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants.

[0132] According to any of the foregoing provisions, the working fluid comprises one or more rare gases, and the one or more rare gases include helium, xenon, or combinations thereof.

[0133] According to any of the foregoing clauses, the undesirable gas includes at least carbon oxides (CO). X ).

[0134] The system according to any of the foregoing clauses, wherein the one or more gas capture systems include adsorbent-based gas capture systems, solvent-based gas capture systems, cryogenic gas capture systems, or combinations thereof.

[0135] The system according to any of the foregoing clauses, wherein the heat source includes a nuclear system having a nuclear reactor.

[0136] The system according to any of the foregoing clauses, wherein the heat source includes a solar thermal system having one or more solar collectors.

[0137] The system according to any of the foregoing clauses, wherein the heat source includes a combustion system.

[0138] The system according to any of the foregoing clauses includes the heat source connected to the steam generator, the steam turbine connected to the steam generator, and the generator connected to the steam turbine.

[0139] According to any of the foregoing provisions, the thermodynamic cycle includes a closed-loop Brayton cycle, the heat source includes a nuclear system or a solar thermal system, the undesirable gas includes carbon dioxide (CO2), the one or more gas capture systems include an adsorbent-based gas capture system, and the working fluid includes a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

[0140] A system includes a controller having a memory, a processor, and instructions stored in the memory and executable by the processor to control a direct air capture (DAC) system comprising one or more gas capture systems to capture unwanted gases from the air. The processor of the controller is also configured to control a thermodynamic cycle to provide heat to the one or more gas capture systems. The thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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.

[0141] According to the system described in the foregoing clauses, the thermodynamic cycle includes a closed-loop Brayton cycle, the heat source includes a nuclear system or a solar thermal system, the undesirable gas includes carbon dioxide (CO2), the one or more gas capture systems include an adsorbent-based gas capture system, and the working fluid includes a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

[0142] A method includes controlling a direct air capture (DAC) system comprising one or more gas capture systems to capture unwanted gases from the air. The method also includes controlling a thermodynamic cycle to provide heat to the one or more gas capture systems. The thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger. The fluid loop 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.

[0143] According to the methods described in the foregoing clauses, the thermodynamic cycle includes a closed-loop Brayton cycle, the heat source includes a nuclear system or a solar thermal system, the undesirable gas includes carbon dioxide (CO2), the one or more gas capture systems include an adsorbent-based gas capture system, and the working fluid includes a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

[0144] This written description uses examples to disclose the invention, including the best mode, and also enables any person skilled in the art to practice the invention, including making and using any device or system and performing any of the included methods. The patentable scope of the invention is defined by the claims and may include other examples that would occur to a person skilled in the art. Such other examples are contemplated within the scope of the claims if they have structural elements that are not different from the literal language of the claims, or if they include equivalent structural elements that are not substantially different from the literal language of the claims.

Claims

1. A system comprising: A direct air capture (DAC) system, the direct air capture (DAC) system comprising one or more gas capture systems configured to capture unwanted gases from the air; and A thermodynamic cycle comprising a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger, wherein the fluid loop 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.

2. The system of claim 1, wherein the system comprises a heat storage system having one or more heat storage media configured to store heat from the thermodynamic cycle and selectively supply the heat to the one or more gas capture systems.

3. The system according to claim 2, wherein the one or more thermal storage media comprises sensible thermal energy storage, latent thermal energy storage and / or thermochemical thermal energy storage.

4. The system of claim 2, wherein the one or more thermal storage media comprises one or more phase change materials.

5. The system of claim 1, wherein the working fluid comprises a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

6. The system of claim 1, wherein the working fluid comprises a supercritical fluid.

7. The system of claim 6, wherein the supercritical fluid comprises supercritical carbon dioxide (CO2).

8. The system of claim 7, wherein the supercritical CO2 comprises one or more dopants, and the one or more dopants comprise sulfur dioxide (SO2), hexafluorobenzene (C6F6), titanium tetrachloride (TiCl4), or any combination of dopants.

9. The system of claim 1, wherein the working fluid comprises one or more rare gases, and the one or more rare gases comprise helium, xenon, or combinations thereof.

10. The system of claim 1, wherein the undesirable gas comprises at least carbon oxides (CO). X ).

11. The system of claim 1, wherein the one or more gas capture systems comprise an adsorbent-based gas capture system, a solvent-based gas capture system, a cryogenic gas capture system, or a combination thereof.

12. The system of claim 1, wherein the heat source comprises a nuclear system having a nuclear reactor.

13. The system of claim 1, wherein the heat source comprises a solar thermal system having one or more solar collectors.

14. The system of claim 1, wherein the heat source comprises a combustion system.

15. The system of claim 1, wherein the system comprises the heat source connected to the steam generator, the steam turbine connected to the steam generator, and the generator connected to the steam turbine.

16. The system of claim 15, wherein the thermodynamic cycle comprises a closed-loop Brayton cycle, the heat source comprises a nuclear system or a solar thermal system, the undesirable gas comprises carbon dioxide (CO2), the one or more gas capture systems comprise an adsorbent-based gas capture system, and the working fluid comprises a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

17. A system comprising: The controller has a memory, a processor, and instructions, the instructions being stored in the memory and executable by the processor to: Control a direct air capture (DAC) system that includes one or more gas capture systems to capture unwanted gases from the air; and A thermodynamic cycle is controlled to provide heat to the one or more gas capture systems, wherein the thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger, wherein the fluid loop 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.

18. The system of claim 17, wherein the thermodynamic cycle comprises a closed-loop Brayton cycle, the heat source comprises a nuclear system or a solar thermal system, the undesirable gas comprises carbon dioxide (CO2), the one or more gas capture systems comprise an adsorbent-based gas capture system, and the working fluid comprises a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

19. A method comprising: Control a direct air capture (DAC) system that includes one or more gas capture systems to capture unwanted gases from the air; as well as A thermodynamic cycle is controlled to provide heat to the one or more gas capture systems, wherein the thermodynamic cycle includes a fluid loop having at least one compressor, at least one regenerator, at least one turbine, at least one first heat exchanger, and at least one second heat exchanger, wherein the fluid loop 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.

20. The method of claim 19, wherein the thermodynamic cycle comprises a closed-loop Brayton cycle, the heat source comprises a nuclear system or a solar thermal system, the undesirable gas comprises carbon dioxide (CO2), the one or more gas capture systems comprises an adsorbent-based gas capture system, and the working fluid comprises a supercritical fluid, an inert gas, a rare gas, an organic fluid, or any combination thereof.

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