Carbon dioxide capture and separation system utilizing heat pumps for thermal recuperation and steam generation

Abstract

This invention relates a carbon dioxide (CO2) capture and separation system (CCSS) and method for removing CO2 from the air while recuperating process heat for improved thermal efficiency. At least one reactor containing a solid sorbent is exposed to ambient air, whereby the solid sorbent adsorbs CO2 from the air. The solid sorbent undergoes a steam-assisted temperature-vacuum swing adsorption process using steam for heating and purging. The steam is generated by a heat pump through which an aqueous heat transfer fluid circulates. The heat transfer fluid is warmed using a heat exchanger, and the heat exchanger is warmed using ambient air or exhaust air recirculated from the at least one reactor. Recirculating the heat transfer fluid within condensers downstream of the at least one reactor captures waste heat during the process of separating CO2 from steam.

Description

Patent ApplicationAttorney Docket No.: 235.0017-WO00CARBON DIOXIDE CAPTURE AND SEPARATION SYSTEM UTILIZING HEAT PUMPS FOR THERMAL RECUPERATION AND STEAM GENERATIONCROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims priority to U.S. Provisional Application No. 63 / 692,354, filed on September 9, 2024; the disclosure of which is incorporated herein by reference.TECHNICAL FIELD

[0002] The invention relates to systems and methods for direct air capture of carbon dioxide (CO2). More specifically, the invention relates to a steam-assisted temperature-vacuum swing adsorption (TVSA) process that utilizes heat pumps as a source of thermal energy for generating steam and for transferring heat to and from solid sorbent materials housed in reactors that adsorb CO2from the atmosphere.BACKGROUND

[0003] Global warming is posing devastating effects on our climate, health, and communities. Coastal flooding due to rising sea levels, extended wildfire seasons, as well as more destructive hurricanes are the direct impacts of climate change. Moreover, global food and water security are at stake. Global warming is directly linked to the increase in the level of greenhouse gases in the atmosphere. Carbon dioxide (CO2) is a major greenhouse gas, and its concentration in the atmosphere has sharply increased over the past century due to the burning of fossil fuels. Although efforts are underway to move toward renewable energy sources that do not emit greenhouse gases, shifting our energy supply to completely renewable sources is not possible in the near term and requires further technological advancements and significant global investments. In the meantime, the 2022 IPCC report makes clear that the world is not on a trajectory to limit global warming above the 1.5 C threshold by 2050, and that to stave off the worst effects of climate disaster, a means to remove CO2from the atmosphere must exist in the future. Therefore, there is a growing need for technologies that can efficiently capture CO2from the flue gas of power plants and other industrial processes and, increasingly, even from ambient air. The latter technology is known as direct air capture (DAC).

[0004] CO2capture processes commonly utilize some type of regenerable adsorbent bed to capture the CO2from a gas or air stream (see, for example, Sanz-Perez, et al., Chemical Reviews, 2016, 116, 11840- 11876, which is incorporated herein by reference in its entirety). A common approach involves an initial step of moving ambient air or flue gas through a bed of a solid sorbent that is effective at capturing aPatent ApplicationAttorney Docket No.: 235.0017-WO00 significant portion of the CO? contained therein. Once the sorbent reaches a level of significant saturation of CO2, it needs to be regenerated in a subsequent step. During regeneration, the adsorbent bed is treated with, for example, heat, vacuum, steam, or some combination thereof to cause the CO2to desorb from the sorbent. The released CO2is subsequently purged from the reactor and captured, and the regenerated sorbent can then be cooled and returned to the first step and reused to capture more CO2. Due to the relatively low concentrations of CO2in ambient air (though still incredibly high by historical standards: currently 425 parts per million), high volumes of ambient air need to be moved and processed in a DAC process. Moreover, additional energy is required to regenerate the sorbent, so the systems need to be highly efficient.

[0005] Common solid CO2sorbents include various zeolites or molecular sieves; amine-functionalized siliceous, inorganic, activated carbon, graphitic, metal organic framework (MOF) or polymeric supports; amine-functionalized carbon, glass, cellulosic, or polymeric fibers; and basic or weakly basic ion exchange resins. In some cases, the solid CO2sorbents are utilized in powder or pellet form in fluidized bed or packed bed configurations through which air is passed. In other cases, the solid CO2sorbents are utilized in fibrous webs, mats, or woven fabrics through which air is passed. In still other cases, the solid CO2sorbents are formed into structured monoliths or other structured forms such as sheets, films, membranes, or plates through or around which air may pass. Sorbents structured in a sheet-type form may be conveniently mounted within a supporting cartridge to form parallel-plate contactor structures which may be mounted within an adsorbent reactor chamber. Gases and / or fluids may then be flowed through the contactor structures with a lower pressure drop compared with, for example, packed bed configurations.

[0006] The captured CO2is desorbed during the sorbent regeneration process, which usually involves some combination of applying heat and vacuum to the adsorbent bed to effect desorption. This process is commonly known as temperature-vacuum swing adsorption (TVSA) and has been researched and reported in the literature (see, for example, Elfving, et al., Chemical Engineering Journal, 2021, 404, 126337, which is incorporated herein by reference in its entirety). A particular version, known in the art as steam-assisted TVSA, utilizes heat from steam, flowing steam through the adsorbent bed to efficiently transfer heat to the adsorbent bed as described in, for example, U.S. Patent No. 4,822,383 (Brose, et al.) Li, et al., ChemSusChem, 2010, 3, 899-903; Wijesiri, et al., Industrial & Engineering Chemistry Research, 2019, 58, 15606-15618; and Bos, et al., Chemical Engineering Science: X, 2019, 2, 100020; which are each incorporated herein by reference in their entirety. Steam is also an effective carrier to sweep away gaseous CO2as it is being desorbed, thereby promoting increased desorption by way ofPatent ApplicationAttorney Docket No.: 235.0017-WO00 reducing the partial pressure of the gas above the sorbent as described in, for example, U.S. Patent No.10,279,306 (Gebald, et al.), which is incorporated herein by reference in its entirety.

[0007] Steam-assisted TVSA processes require substantial amounts of power and energy to repeatedly heat sorbent and desorb CO2, and prior art traditionally relied on electricity to generate steam as a major source of process heat and as a carrier to sweep away gaseous CO2as it is being desorbed. See, for example, U.S. Patent No. 10,279,306 (Gebald, et al.). However, the capital cost for the power system equipment and the operating costs to generate electricity significantly increase the levelized costs of carbon capture technology, and the carbon-offsetting potential of direct air carbon capture is inherently limited by a carbonized electric grid run using fossil fuels. There is a need for improved direct air CO2capture and separation systems and methods that use significantly less electricity and power.

[0008] Heat pumps are known in the art to reduce the power requirements of heating. They can also reduce the power requirements of generating the steam needed to run the steam-assisted TVSA process. Typical heat pumps use a refrigeration cycle driven by electricity to extract heat from sources such as ambient air, ground, water, or process fluids. The heat is transferred into a heat transfer fluid which is compressed and elevated to a higher temperature, where it can deliver heat to a higher- temperature sink such as a steam boiler. Heat pumps reduce the amount of energy required to provide heat to a system by moving heat, which can be more efficient than generating heat using electricity or a fuel source. Heat pumps can also act bidirectionally and act as chillers or air conditioners due to the removal of heat energy from the low-temperature fluid stream.

[0009] One specific type of heat pump is a mechanical vapor compression heat pump. Vapor compression heat pumps function by using electric-driven compressors to compress a vaporized refrigerant or heat transfer fluid into a liquid; the phase change releases heat when the vapor condenses, and that heat is transferred to a heat sink. Pressure-reducing expansion valves inside the heat pump subsequently expand the condensed refrigerant or heat transfer fluid to a lower pressure, thereby producing a cooler mixture of vapor and liquid. When that cooler refrigerant or heat transfer fluid mixture then encounters an external heat source, the resulting transfer of heat fully evaporates the remaining vapor and the refrigerant or heat transfer fluid is routed back to the compressor, where it is compressed again to restart the cycle. The external heat source can come from the ambient environment, or it can be the waste heat from another thermodynamic industrial process.

[0010] DAC systems can incorporate heat pumps to plant and heat transfer processes to reduce the fuel and electricity costs required to generate steam for the concomitant heating and purging of sorbent material. Traditional electric boilers use steam to generate electricity, but each kilowatt-hour (kWh) ofPatent Application Attorney Docket No.: 235.0017-WO00 heat for generating the steam requires at least one kWh of electrical energy. A heat pump requires less than one kWh of electrical energy for each kWh of heat required to generate steam. Using heat pumps instead of boilers to make the steam in a steam-assisted TVSA process can, therefore, reduce the energy usage, operating costs, and carbon emissions of a CO2capture and separation system.

[0011] Methods have been developed to recover heat from the steam-assisted TVSA process. U.S Patent No. 10,279,306 (Gebald et al.), which is incorporated herein by reference in its entirety, discloses the basic approach of incorporating steam to assist in the desorption, which also embodies the use of either a heat pump or vapor re-compressor and kettle re-boiler to recover the heat of steam condensation for use in steam generation. The disadvantage of using a heat pump in the range of temperature of interest of Gebald et al. is the lack of practical working fluids for the heat pump. The heat pump would be limited to using certain hydrocarbons such as butane, which introduces extra costs for equipment to prevent or mitigate hazards associated with inhalation and fire. Gebald et al. also discloses a heat exchanger embedded in the sorbent structure, for indirectly heating and cooling the sorbent. The incorporation of an embedded heat exchanger adds cost, complicates fabrication, adds risk of unintended leakage of the heat transfer fluid, produces a non-uniform temperature distribution in the sorbent and surrounding structure, and makes removal and replacement of the sorbent more difficult and time consuming. Finally, Gebald et al. fails to disclose a means to recover the sensible heat needed to raise the temperature of the sorbent.

[0012] There is a need for improved direct air CO2capture and separation systems and methods that use significantly less electricity and power. While heat pumps can be beneficial to DAC systems as a direct replacement to boilers, the performance of a heat pump-assisted system can often be further improved by various designs and operation techniques. Examples include routing waste heat from the DAC process or an external process into the heat pump heat source, incorporating accumulators to enable more consistent outflow, and distributing a plurality of heat pumps rather than centralizing steam production to facilitate steam generation at a lower pressure. These concepts can improve the energy efficiency, reliability, adaptability, and ease of use of a heat pump system paired with a DAC system.SUMMARY

[0013] The invention relates to a system and method for capturing carbon dioxide (CO2) from the air using CO2-adsorbent material (also called "sorbent") and separating CO2from a product stream in a CO2capture and separation system (CCSS). The system and method in accordance with the inventionPatent ApplicationAttorney Docket No.: 235.0017-WO00 comprises at least one heat pump for providing the heat necessary to boil water into steam, providing for more efficient steam-assisted temperature vacuum swing adsorption (TVSA) of the sorbent by obviating the need for traditional boilers. A distinct improvement offered by the invention is the incorporation of at least one air-heated heat exchanger in the refrigeration cycle of a heat transfer fluid, wherein the heat transfer fluid delivers heat to the at least one heat pump.

[0014] The invention further relates to a CCSS comprising at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network; a heat pump; a process stream comprising water and disposed in the piping network, wherein the heat pump delivers heat to the process stream to generate steam; a heat transfer fluid disposed in the piping network, wherein the heat pump receives heat from the heat transfer fluid; at least one storage tank for storing heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger delivers heat to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump fluidly connected to the at least one condensate tank for delivering water from the at least one condensate tank to the process stream.

[0015] The invention further relates to a CCSS comprising at least one DAC module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump fluidly connected to the at least one DAC module, wherein the heat pump is configured to generate steam, and wherein the heat pump comprises: a refrigerant; an expansion valve for reducing a pressure of the refrigerant; a compressor for increasing the pressure of the refrigerant; an evaporator for vaporizing the refrigerant; and a heat pump condenser disposed in the piping network configured to transfer heat from the refrigerant to a process stream comprising water, wherein the heat pump is fluidly connected to the at least one DAC module via the piping network. The CCSS further comprises a heat transfer fluid disposed in the piping network, wherein the evaporator receives heat from the heat transfer fluid; at least one storage tank for storing the heat transfer fluid, wherein the at least one storage tank is fluidlyPatent ApplicationAttorney Docket No.: 235.0017-WO00 connected to the heat pump; at least one cooling pump fluidly connected to the at least one DAC module that acts to cool the at least one solid sorbent; at least one air evacuation pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module, wherein the at least one condenser condenses steam into condensate; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger transfers heat from ambient air to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump for delivering water from the at least one condensate tank to the process stream.

[0016] The invention further relates to a CCSS comprising at least one DAC module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump comprising a heat pump evaporator and a heat pump condenser, wherein the heat pump is fluidly connected to a steam accumulator and the at least one DAC module via the piping network, wherein the heat pump condenser outputs condensed water to the steam accumulator as steam, and wherein the heat pump condenser outputs a heat transfer fluid to the at least one DAC module; the heat transfer fluid disposed in the piping network, wherein the heat transfer fluid flows through the heat pump evaporator and delivers heat to the heat pump; at least one auxiliary steam condenser fluidly connected to the at least one DAC module, wherein the at least one DAC module outputs a mixture of steam and CO2to the at least one auxiliary steam condenser; at least one separator fluidly connected to the at least one auxiliary steam condenser, wherein the at least one separator separates the product stream into CO2and water; and an air-heated heat exchanger fluidly connected to the heat pump and the at least one auxiliary steam condenser, wherein: the air-heated heat exchanger is heated using exhaust air output from the at least one DAC module; the heat transfer fluid flows through the air-heated heat exchanger via the piping network; and the air-heated heat exchanger delivers heat to the heat transfer fluid.

[0017] The CCSS of the invention may further comprise all or one of an auxiliary heat source, a vapor re-compressor, a plurality of heat pumps, and a steam accumulator. In some embodiments of the invention, the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume. In some embodiments of the invention, the at least one solid sorbent is a one of a zeolite or amine- functionalized compound such as amine-functionalized siliceous, inorganic, activated carbon, graphitic,Patent ApplicationAttorney Docket No.: 235.0017-WO00 metal organic framework (MOF) or polymeric compounds. In some embodiments of the invention, the at least one solid sorbent is amine-functionalized carbon, glass, cellulosic, or polymeric fibers. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine impregnated onto a porous support such as silica, alumina, or activated carbon. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine grafted onto a porous support such as silica, alumina, or mesoporous materials like SBA-15 or MCM-41. In some embodiments of the invention, the at least one solid sorbent is a basic or weakly basic ion exchange resin. In some embodiments of the invention, the at least one solid sorbent is a MOF, a porous organic polymer, a covalent organic framework (COF), a porous aromatic framework (PAF), or a hypercrosslinked polymer. In some embodiments of the invention, the at least one solid sorbent is formed as a powder, pellet, fluidized bed, packed bed, fibrous web, fibrous mat, woven fabric, structured monolith, sheet, film, membrane, or plate. In some embodiments of the invention, the at least one solid sorbent is containerized within a support cartridge to form parallel-plate structures or vertical stacks.

[0018] The invention further relates to a method of capturing CO2, comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2 from the ambient air; delivering heat to a heat transfer fluid using a heat exchanger, wherein the heat exchanger delivers heat from ambient air to the heat transfer fluid; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the at least one solid sorbent in the at least one evacuated reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2to create a product mixture of steam and CO2; directing the product mixture of steam and CO2 from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2 in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

[0019] The invention further relates to a method of capturing CO2, comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air, and wherein the ambient air exits the at least one reactor as exhaust after making contact with the at least one solid sorbent; directing a portion of thePatent ApplicationAttorney Docket No.: 235.0017-WO00 exhaust to a heat exchanger through which flows a heat transfer fluid, wherein the portion of exhaust warms the heat transfer fluid inside the heat exchanger; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the at least one solid sorbent in the at least one reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2 inside the at least one reactor to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

[0020] In some embodiments of the invention, the steam generated by the at least one heat pump exhibits a pressure of at least 1.0 bar and a temperature of at least 100° C.

[0021] In some embodiments of the invention, the method steps are repeated and staggered using a plurality of subsets of reactors, and wherein one subset of reactors simultaneously undergoes a different step than another subset of reactors.

[0022] In some embodiments of the invention, a subset of reactors undergoes the step of directing ambient air through the at least one reactor containing the solid sorbent while another subset of reactors undergoes the step of heating the solid sorbent to a temperature between 80° and 100° C.

[0023] In some embodiments of the invention, the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume.

[0024] In some embodiments of the invention, the at least one solid sorbent is a zeolite or amine- functionalized compound.BRIEF DESCRIPTION OF THE DRAWINGS

[0025] These and other objects, features, and advantages of the invention will be more fully appreciated or become better understood when considered in conjunction with the accompanying drawings, where:

[0026] FIG. 1 shows an exemplary mechanical heat pump comprising a refrigerant in accordance with the prior art.Patent ApplicationAttorney Docket No.: 235.0017-WO00

[0027] FIG. 2A shows an exemplary carbon dioxide (CO?) capture and separation system (CCSS) in accordance with the invention.

[0028] FIG. 2B shows inlet and outlet material flows of the exemplary CCSS of FIG. 2A in accordance with the invention.

[0029] FIG. 2C shows an exemplary direct air capture (DAC) module in accordance with the invention.

[0030] FIG. 3 shows an exemplary CCSS wherein heat is recaptured from DAC module exhaust in accordance with the invention.

[0031] FIG. 4 shows an exemplary CCSS comprising an auxiliary heat source in a heat transfer fluid loop of a piping network in accordance with the invention.

[0032] FIG. 5 shows an exemplary CCSS comprising a mechanical vapor re-compressor in accordance with the invention.

[0033] FIG. 6 shows an exemplary CCSS comprising a plurality of heat pumps in accordance with the invention.

[0034] FIG. 7 shows an exemplary reactor in accordance with the invention.

[0035] FIG. 8 shows an exemplary method of a steam-assisted temperature-vacuum swing adsorption (TVSA) process for capturing CO2in accordance with the invention.DETAILED DESCRIPTION

[0036] The invention relates to a carbon dioxide (CO2) capture and separation system (CCSS) comprising a plurality of components connected in a network that forms a carbon capture and separation cycle. The network of the CCSS may comprise a piping network, and the piping network may comprise a plurality of pipes, valves, or any other suitable pathways for diverting, routing, filtering, or separating liquid or gas fluids to, from, and between components of the CCSS. In all exemplary embodiments of the CCSS in accordance with the invention, components of the CCSS may be described as being "fluidly connected" and / or "directly connected". In this context, "fluidly connected" means that the system components share a piping network that allows fluid streams to flow between components. "Directly connected" means that the system components share a piping network that links the two components via a direct physical connection. Components described as directly connected may also be fluidly connected, and components described as fluidly connected may also be directly connected. Two components with interstitial elements between them in the piping network, wherein a fluid can flow through both components as well as through the interstitial element, can also be fluidly connected. Intermittent cessation of fluid movement via a valve or door does not imply a lack of a fluid connection betweenPatent ApplicationAttorney Docket No.: 235.0017-WO00 components.

[0037] A mechanical heat pump is known in the state of the art as a means for conducting heat transfer for the industrial generation of steam. An example of a typical mechanical heat pump known in the art is shown in FIG. 1. Heat pump 100 comprises a mechanical compressor 101 that is powered, such as by an electrical input, to perform work on a refrigerant 108 that is routed through constituent elements of the heat pump 100 as part of a thermal cycle. The refrigerant 108, in a low-pressure state, receives heat from a heat transfer fluid 107 inside evaporator 104. The heat transfer fluid 107 vaporizes the refrigerant 108 before passing it to the mechanical compressor 101. The mechanical compressor 101 compresses the refrigerant 108 to increase its pressure and temperature before passing the refrigerant 108 to condenser 102. The condenser 102 delivers heat from the refrigerant 108, in a high-pressure state, to feedwater 105 in a process stream. The heat from the condenser 102 boils the feedwater 105 into steam 106. The refrigerant 108, having lost temperature in the heat transfer, is then routed to expansion valve 103, which increases the pressure of the refrigerant 108 before passing it back to the evaporator 104 and completing the thermal cycle. In this manner, heat transfer fluid heats a refrigerant 108, which is made hot enough by the mechanical compressor 101 to boil feedwater 105 passing through the condenser 102 into steam 106. Throughout the disclosure, when a heat pump is described as "generating steam" or "heating a process stream so as to generate steam", the thermal cycle shown in FIG. 1 is taking place.

[0038] The invention relates to a CCSS for removing CO2from the atmosphere comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network; a heat pump; a process stream comprising water and disposed in the piping network, wherein the heat pump delivers heat to the process stream to generate steam; a heat transfer fluid disposed in the piping network, wherein the heat pump receives heat from the heat transfer fluid; at least one storage tank for storing heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at leastPatent ApplicationAttorney Docket No.: 235.0017-WO00 one separator separates the product stream into CO2 and water; at least one condenser fluidly connected to the at least one DAC module; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger delivers heat to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump fluidly connected to the at least one condensate tank for delivering water from the at least one condensate tank to the process stream.

[0039] The invention further relates to a CCSS for removing CO2from the atmosphere comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump fluidly connected to the at least one DAC module, wherein the heat pump is configured to generate steam, and wherein the heat pump comprises: a refrigerant; an expansion valve for reducing a pressure of the refrigerant; a compressor for increasing the pressure of the refrigerant; an evaporator for vaporizing the refrigerant; and a heat pump condenser disposed in the piping network configured to transfer heat from the refrigerant to a process stream comprising water, wherein the heat pump is fluidly connected to the at least one DAC module via the piping network; a heat transfer fluid disposed in the piping network, wherein the evaporator receives heat from the heat transfer fluid; at least one storage tank for storing the heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one cooling pump fluidly connected to the at least one DAC module that acts to cool the at least one solid sorbent; at least one air evacuation pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module, wherein the at leastPatent ApplicationAttorney Docket No.: 235.0017-WO00 one condenser condenses steam into condensate; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger transfers heat from ambient air to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump for delivering water from the at least one condensate tank to the process stream.

[0040] In some embodiments of the invention, the CCSS further comprises an auxiliary heat source. In some embodiments of the invention, the auxiliary heat source is disposed in the piping network between the at least one condenser and the heat pump. In some embodiments of the invention, the auxiliary heat source is fluidly connected to the at least one condenser and the at least one storage tank that stores the heat transfer fluid. In some embodiments of the invention, the auxiliary heat source warms the heat transfer fluid before it flows to the at least one storage tank and the heat pump.

[0041] In some embodiments of the invention, the CCSS further comprises a vapor re-compressor. In some embodiments of the invention, the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one pump. In some embodiments of the invention, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one pump, and the at least one DAC module. In some embodiments of the invention, the vapor re-compressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

[0042] In some embodiments of the invention, the CCSS further comprises a vapor re-compressor. In some embodiments of the invention, the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one cooling pump. In some embodiments of the invention, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one cooling pump, and the at least one DAC module. In some embodiments of the invention, the vapor recompressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

[0043] The invention further relates to CCSS for removing CO? from the atmosphere comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO? from the air and desorbing CO? into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump comprising a heat pump evaporator and a heat pump condenser, wherein the heatPatent ApplicationAttorney Docket No.: 235.0017-WO00 pump is fluidly connected to a steam accumulator and the at least one DAC module via the piping network, wherein the heat pump condenser outputs condensed water to the steam accumulator as steam, and wherein the heat pump condenser outputs a heat transfer fluid to the at least one DAC module; the heat transfer fluid disposed in the piping network, wherein the heat transfer fluid flows through the heat pump evaporator and delivers heat to the heat pump; at least one auxiliary steam condenser fluidly connected to the at least one DAC module, wherein the at least one DAC module outputs a mixture of steam and CO2to the at least one auxiliary steam condenser; at least one separator fluidly connected to the at least one auxiliary steam condenser, wherein the at least one separator separates the product stream into CO2and water; and an air-heated heat exchanger fluidly connected to the heat pump and the at least one auxiliary steam condenser, wherein: the air-heated heat exchanger is heated using exhaust air output from the at least one DAC module; the heat transfer fluid flows through the air-heated heat exchanger via the piping network; and the air-heated heat exchanger delivers heat to the heat transfer fluid.

[0044] In some embodiments of the invention, the CCSS further comprises a steam accumulator. In some embodiments of the invention, the steam accumulator is fluidly connected to the heat pump and the at least one DAC module, wherein steam that exits the heat pump flows into the steam accumulator and steam from the steam accumulator flows into the at least one DAC module. In some embodiments of the invention, the delivery of steam from the steam accumulator to the at least one DAC module is dynamically adjusted depending on the number of the at least one DAC module or at least one reactor which are opened or closed for the respective adsorption and desorption of CO2by the at least one solid sorbent. The exemplary embodiments illustrated by the drawings show steam accumulators as comprising steam, however, the CCSS of the invention and the exemplary embodiments may have steam accumulators that store steam in addition to a portion of condensed liquid water collected on the bottom of the accumulators.

[0045] In some embodiments of the invention, the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume. In some embodiments of the invention, the at least one solid sorbent is a one of a zeolite or amine-functionalized compound such as amine-functionalized siliceous,Patent ApplicationAttorney Docket No.: 235.0017-WO00 inorganic, activated carbon, graphitic, metal organic framework (MOF) or polymeric compounds. In some embodiments of the invention, the at least one solid sorbent is amine-functionalized carbon, glass, cellulosic, or polymeric fibers. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine impregnated onto a porous support such as silica, alumina, or activated carbon. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine grafted onto a porous support such as silica, alumina, or mesoporous materials like SBA-15 or MCM-41. In some embodiments of the invention, the at least one solid sorbent is a basic or weakly basic ion exchange resin. In some embodiments of the invention, the at least one solid sorbent is a MOF, a porous organic polymer, a covalent organic framework (COF), a porous aromatic framework (PAF), or a hypercrosslinked polymer. In some embodiments of the invention, the at least one solid sorbent is formed as a powder, pellet, fluidized bed, packed bed, fibrous web, fibrous mat, woven fabric, structured monolith, sheet, film, membrane, or plate. In some embodiments of the invention, the at least one solid sorbent is containerized within a support cartridge to form parallel-plate structures or vertical stacks.

[0046] The exemplary embodiments illustrated by the drawings show a plurality of DAC modules, however, the CCSS of the invention and the exemplary embodiments may have at least one DAC module. In some embodiments of the invention, the CCSS of the inventions as exemplified in the drawings have one DAC module.

[0047] An exemplary embodiment of a CCSS in accordance with the invention is shown in FIG. 2A. The CCSS comprises a heat pump 1, wherein the heat pump 1 comprises a refrigerant, a heat pump condenser 2 for increasing the pressure of the refrigerant, and a heat pump evaporator 19 for evaporating the refrigerant. In some embodiments of the invention, the heat pump 1 is a mechanical heat pump further comprising an expansion valve (not shown) for reducing the pressure of the refrigerant and a compressor (not shown) for increasing the pressure of the refrigerant. In some embodiments of the invention, the heat pump 1 is powered by an electrical input to power the compressor.

[0048] The CCSS further comprises a steam accumulator 3, a feedwater pump 18, a first storage tank 20, a second storage tank 24, and a plurality of direct air capture (DAC) modules 6. The heat pump condenser 2 is fluidly connected to the steam accumulator 3 and the feedwater pump 18. The heat pump evaporator 19 is fluidly connected to the first storage tank 20 and is fluidly connected to the second storage tank 24, via a second heat transfer fluid pump 25. The first storage tank 20 and the second storage tank 24 serve as repositories and distribution nodes for a heat transfer fluid 21. ThePatent ApplicationAttorney Docket No.: 235.0017-WO00 steam accumulator 3 is fluidly connected to at least one of the plurality of DAC modules 6. The steam accumulator 3 is configured to serve as a repository and distribution node for steam 4.

[0049] The exemplary CCSS shown in FIG. 2A further comprises a first steam condenser 10, a second steam condenser 14, an air-heated heat-exchanger 23, a first separator 11, and a second separator 15. The first steam condenser 10 is fluidly connected to at least one of the plurality of DAC modules 6, the second steam condenser 14, the second storage tank 24, and the first separator 11. The second steam condenser 14 is fluidly connected to the first steam condenser 10, the first separator 11, and the second separator 15. The air-heated heat exchanger 23 is fluidly connected to the heat pump 1 and at least one of the first steam condenser 10 and the second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the first steam condenser 10 (not shown in FIG. 2A). In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is fluidly connected to both the first steam condenser 10 and the second steam condenser 14.

[0050] The exemplary CCSS shown in FIG. 2A further comprises a first heat transfer fluid pump 22. In some embodiments of the invention, the air-heated heat exchanger 23 is heated using ambient air 29 that flows over the air-heated heat exchanger 23, either through passive flow or induced flow, such as via fans or blowers. The heat transfer fluid 21 flows through the air-heated heat exchanger 23 via a piping network from the first storage tank 20 and is pumped from the first storage tank 20 to the airheated heat exchanger 23 via the first heat transfer fluid pump 22. The first heat transfer fluid pump 22 is fluidly connected to the first storage tank 20 and the air-heated heat exchanger 23. The heat transfer fluid 21 is heated via the air-heated heat exchanger 23 prior to passing into the second steam condenser 14. The transfer of heat from the heat transfer fluid 21 also vaporizes the refrigerant in the heat pump evaporator 19. The hot refrigerant subsequently facilitates steam generation when the heat pump condenser 2 boils feedwater in a process stream passing through the heat pump 1.

[0051] The first separator 11 and the second separator 15 comprise enclosed containers that separate CO2 product from steam and water via gravity; i.e., gaseous CO2 rises to the top of the separator container while liquid condensate (condensed water) falls to the bottom. After a desorption step and a purge step of a steam-assisted temperature-vacuum swing adsorption (TVSA) process, a mixture of CO2 and steam is directly output from the plurality of DAC modules 6, and this output steam is condensed into water via the first steam condenser 10 and the second steam condenser 14.

[0052] The first storage tank 20 and the second storage tank 24 are configured to store the heatPatent ApplicationAttorney Docket No.: 235.0017-WO00 transfer fluid 21. The first storage tank 20 contains cold liquid heat transfer fluid 21 and the second storage tank 24 contains hotter liquid heat transfer fluid 21. In some embodiments of the invention, the first storage tank 20 and the second storage tank 24 are each independently combined storage tanks, stratified storage tanks, or layered charge storage tanks. Stratified or layered storage tanks may comprise vertical line valves and heating elements distributed along the height of the storage tank for removing and adding fluids of differing states of matter and temperature while minimizing mixing of disparate fluids.

[0053] In some embodiments of the invention, the CCSS comprises a plurality of pumps. The plurality of pumps are configured to force fluid flow through the piping network and between system components. The exemplary CCSS shown in FIG. 2A further comprises the feedwater pump 18, a condensate tank 8, a first condensate pump 13, and a second condensate pump 16. The feedwater pump 18 is fluidly connected to the condensate tank 8 and the heat pump 1. The feedwater pump 18 is configured to pump condensate 9 to the heat pump 1. The first condensate pump 13 is fluidly connected to the first separator 11 and is configured to pump condensate 9 from the first separator 11 to the condensate tank 8. The second condensate pump 16 is fluidly connected to the second separator 15 and is configured to pump condensate 9 from the second separator 15 to the condensate tank 8. The exemplary CCSS shown in FIG 2A further comprises a cooling pump 17, which is fluidly connected to at least one of the plurality of DAC modules 6 and the second steam condenser 14. In some embodiments of the invention, the cooling pump 17 is a vacuum pump that evacuates the plurality of DAC modules 6 during a cooling step of the steam-assisted TVSA process. The exemplary CCSS shown in FIG. 2A further comprises a vacuum pump 26, which is fluidly connected to at least one of the plurality of DAC modules 6. The vacuum pump 26 extracts air from the plurality of DAC modules 6 during an air evacuation step of the steam-assisted TVSA process as evacuated air 28. The exemplary CCSS of FIG. 2A further comprises a boost blower 12 which extracts product CO? 1 from the second separator 15 where it can be utilized by another industrial process or sequestered to offset carbon emissions. The exemplary CCSS shown in FIG. 2A further comprises the first heat transfer fluid pump 22 and the second heat transfer fluid pump 25. The first heat transfer fluid pump 22 is fluidly connected to the first storage tank 20 and the air-heated heat exchanger 23 and is configured to pump the heat transfer fluid 21 out of the first storage tank 20. The second heat transfer fluid pump 25 is fluidly connected to the second storage tank 24 and the heat pump evaporator 19 of the heat pump 1 and is configured to pump the heat transfer fluid 21 out of the second storage tank 24. Colder heat transfer fluid 21 from the first storage tank 20 is pumped into the air-heated heat exchanger 23 via the first heat transfer fluid pump 22. Hotter heat transfer fluid 21 fromPatent Application Attorney Docket No.: 235.0017-WO00 the second storage tank 24 is pumped into and through the heat pump evaporator 19 of the heat pump1 to the first storage tank 20 via the second heat transfer fluid pump 25.

[0054] The exemplary CCSS shown in FIG. 2A comprises the plurality of DAC modules 6. Each of the plurality of DAC modules 6 comprises at least one reactor. Each of the at least one reactor comprises an openable and sealable cavity containing a sorbent material capable of adsorbing CO2from an air or gas source. In some embodiments of the invention, the sorbent material is a solid sorbent that can be removed from the at least one reactor. Each of the at least one reactor further comprises ingress and egress capacity via which a plurality of fluid streams can enter and exit. The plurality of fluid streams may comprise ambient air, steam, heat transfer fluid, water, or a mixture thereof. In some embodiments of the invention, each of the at least one reactor inside each of the plurality of DAC modules 6 is fluidly connected to a plurality of common or shared inlet and outlet channels through which the plurality of fluid streams may enter or exit. In some embodiments of the invention, the plurality of fluid streams may enter or exit each of the at least one reactor via at least one inlet and outlet valve, inlet and outlet door, inlet and outlet pipe, or other suitable inlet and outlet mechanism. In some embodiments of the invention, the plurality of inlet and outlet channels facilitate transfer of a plurality of fluid streams into or out of the at least one reactor contained within each of the plurality of DAC modules 6 via module inlet valves 5 and module outlet valves 7, as shown in FIG. 2A. In some embodiments of the invention, the inlet and outlet valves may be ball or gate valves, butterfly valves, or other suitable valve alternatives.

[0055] In some embodiments of the invention, the plurality of fluid streams that flow through the components of the CCSS comprise water in various stages, such as liquid water, gaseous steam, and a mixture thereof. In the exemplary embodiment shown in FIG. 2A, condensate 9 is stored in the condensate tank 8 and pumped via the feedwater pump 18 to the heat pump 1, where it is heated by the heat transfer fluid 21 and converted into steam 4. Steam 4 exits the heat pump 1 and is stored in the steam accumulator 3, where it can be diverted into the plurality of DAC modules 6 for heating the sorbent material contained in the at least one reactor during a steam pressurization step of the steam- assisted TVSA process and for removing desorbed CO2during the purge step. This loop of feedwater phase changed into steam is termed the "process stream".

[0056] Downstream of the plurality of DAC modules 6, any water that is condensed inside the first steam condenser 10 and the second steam condenser 14 is deposited inside the first separator 11 and the second separator 15, respectively, as condensate 9. Condensate 9 is then pumped from the first separator 11 via the first condensate pump 13 to the condensate tank 8. Similarly, condensate 9 isPatent ApplicationAttorney Docket No.: 235.0017-WO00 pumped from the second separator 15 via the second condensate pump 16 to the condensate tank 8. Any water that condenses inside the plurality of DAC modules 6, such as condensate 9, is drained and routed back to the condensate tank 8.

[0057] The steam used for pressurization and purging of the at least one reactor in each of the plurality of DAC modules 6 is generated by the heat pump condenser 2 within the heat pump 1, which boils feedwater in the process stream into steam 4 that is then discharged into the steam accumulator 3. In some embodiments of the invention, the steam accumulator 3 may contain a mixture of saturated liquid and saturated water vapor. In some embodiments of the invention, steam output from the heat pump 1 exhibits a pressure between 1.0 bar and 4.7 bar (e.g., between 1.5-4.0 bar, between 2.0-3.5 bar, or between 2.5-3.0 bar) and a temperature between 100°C and 150°C (e.g., between 110°C -140°C, or between 120°C -130°C). Preferably, the steam output from the heat pump 1 is generated at a pressure of at least 1.0 bar and a temperature of at least 100°C., such as a pressure of 1.2 bar and a temperature of 102°C. Steam 4 is stored in the steam accumulator 3 and distributed to the plurality of DAC modules 6 each comprising the at least one reactor undergoing steam pressurization or steam purging. In this way, an unsteady and dynamic flow of steam can be delivered to the at least one reactor in each of the plurality of DAC modules 6 while a steady and constant flow of steam is generated by the heat pump condenser 2 in the heat pump 1.

[0058] In some embodiments of the invention, the heat transfer fluid is a synthetic or organic fluid in various phases of matter, i.e., liquid, gas, or a mixture thereof. In a preferred embodiment, the heat transfer fluid is water mixed with glycol in a particular ratio. In some embodiments of the invention, the heat transfer fluid is a solution comprising water and between 1% and 15% glycol by volume. In some embodiments of the invention, the heat transfer fluid is 95% water and 5% glycol by volume. In some embodiments of the invention, the heat transfer fluid is an aqueous salt solution. As shown in FIG. 2A, heat transfer fluid 21 flows from the heat pump evaporator 19 to the first storage tank 20 and is removed from the first storage tank 20 via the first heat transfer fluid pump 22. The heat transfer fluid 21 that is pumped from the first storage tank 20 is delivered to the air-heated heat exchanger 23. The air-heated heat exchanger 23 can be heated by a variety of sources such as, but not limited to, ambient air 29, exhaust air output from the plurality of DAC modules 6 during an adsorption step of the steam- assisted TVSA process, and evacuated air 28 withdrawn from the plurality of DAC modules 6 during the air evacuation step of the steam-assisted TVSA process. Heat transfer fluid 21 exiting the air-heated heat exchanger 23 flows to the second steam condenser 14 and then to the first steam condenser 10, and then to the second storage tank 24. Heat transfer fluid 21 is finally pumped into the heat pumpPatent Application Attorney Docket No.: 235.0017-WO00 evaporator 19 from the second storage tank 24 via the second heat transfer fluid pump 25, wherein the heat transfer fluid 21 completes a heat transfer cycle. The circulation of the heat transfer fluid 21 between the first storage tank 20 and the second storage tank 24 as well as into and out of the heat pump 1 is continuous given the operation of the first heat transfer fluid pump 22 and the second heat transfer fluid pump 25.

[0059] During the adsorption step of the steam-assisted TVSA process, the plurality of DAC modules 6 and the at least one reactor therein may be opened or positioned to allow ambient air to enter and exit the at least one reactor and contact the sorbent material contained therein. In some embodiments of the invention, a plurality of fans is used to pull ambient air into and through the at least one reactor and over the sorbent material therein, facilitating the adsorption of CO? by the sorbent material from the air. Air that leaves the at least one reactor and the plurality of DAC modules 6 during the adsorption step may be routed from the plurality of DAC modules 6 to the air-heated heat exchanger 23, or it may be exhausted to the environment.

[0060] FIG. 2B shows exemplary inlet and outlet material flows of the plurality of DAC modules 6 of the exemplary CCSS of FIG. 2A. FIG. 2B exemplifies one of the plurality of DAC modules 6; however, the same configuration may be present in all or some of the plurality of DAC modules 6 in the same CCSS. Each of the plurality of DAC modules 6 comprises at least one reactor. In some embodiments of the invention, each of the plurality of DAC modules 6 comprises a first module outlet valve 39, a second module outlet valve 30, a third module outlet valve 31, and fourth module outlet valve 32 as well as a single module inlet valve 5, as shown in FIG. 2B. In some embodiments of the invention, the at least one reactor of each of the plurality of DAC modules 6 is fluidly connected to the first module outlet valve 39, the second module outlet valve 30, the third module outlet valve 31, and fourth module outlet valve 32 as well as the single module inlet valve 5. The module inlet valve 5 facilitates the transfer and introduction of steam from a steam accumulator into the at least one reactor of each of the plurality of DAC modules 6 that is to be heated and subsequently purged of desorbed CO2. The first module outlet valve 39 actuates to allow for an air evacuation pump 26 to evacuate air out of the at least one reactor of each of the plurality of DAC modules 6 during an air evacuation step of a steam-assisted TVSA process. The second module outlet valve 30 actuates to release a fluid mixture of steam and CO2to a second steam condenser 14 via a cooling pump 17 during a cooling step of the steam-assisted TVSA. The third module outlet valve 31 actuates to deliver a mixture of steam and CO2to a first steam condenser 10 during a purge step of the steam-assisted TVSA. The fourth module outlet valve 32 actuates to drain condensate (condensed liquid water) from the at least one reactor of each of the plurality of DACPatent ApplicationAttorney Docket No.: 235.0017-WO00 modules 6 into a drain line that routes to a condensate tank 8.

[0061] In some embodiments of the invention, the first module outlet valve 39 also diverts air evacuated from the at least one reactor of each of the plurality of DAC modules 6 during the air evacuation step to an air-heated heat exchanger. In this alternative embodiment, evacuated air may be pumped via the air evacuation pump 26 to the air-heated heat exchanger, where it transfers heat to a heat transfer fluid pumped from a first storage tank.

[0062] An exemplary DAC module 6 of a CCSS of the invention comprising a plurality of reactors 33 is shown in FIG 2C. FIG. 2C exemplifies one DAC module 6 comprising a plurality of reactors 33; however, in some embodiments of the invention, the plurality of reactors 33 is grouped into a plurality of DAC modules 6 that can be installed in a modular fashion to adjust carbon removal capacity over time. In some embodiments of the invention, each DAC module comprises at least one reactor. In some embodiments of the invention, individual DAC modules 6, such as the one shown in FIG. 2C, can be isolated from a CCSS of the invention by closing the respective module inlet valve 5 and module outlet valves 39, 30, 31, and 32. The module inlet valve 5 facilitates the transfer and introduction of steam from a steam accumulator into the plurality of reactors that is to be heated and subsequently purged of desorbed CO2. A first outlet valve 39 actuates to allow for an air evacuation pump to evacuate air out of the plurality of reactors during an air evacuation step of a steam-assisted TVSA process. A second outlet valve 30 actuates to release a fluid mixture of steam and CO2to a second steam condenser via a cooling pump during a cooling step of the steam-assisted TVSA. A third outlet valve 31 actuates to deliver a mixture of steam and CO2to a first steam condenser during a purge step of the steam-assisted TVSA. A fourth outlet valve 32 actuates to drain condensate from the plurality of reactors into a drain line that routes to a condensate tank. Each of the plurality of reactors 33 houses solid sorbent for capturing CO2.

[0063] An exemplary reactor 33 is shown in FIG. 7. The reactor houses sorbent material for capturing CO2. In some embodiments of the invention, the sorbent material is a solid sorbent. In some embodiments of the invention, the reactor 33 housing the solid sorbent is a vacuum chamber comprising a plurality of walls that form an enclosure, at least one frame 303 defining an opening of the vacuum chamber, at least one door 301 disposed in each of the at least one frame 303, and at least one seal 105 for sealing the at least one door 301 in the at least one frame 303 when closed. In some embodiments of the invention, the at least one door 301 actuates to open and close the vacuum chamber. In some embodiments of the invention, the opening of the vacuum chamber is bisected by a center sill 304 extending from the at least one frame 303. Each reactor 33 comprises thermal insulation attached to the internal faces of the plurality of walls of the vacuum chamber. The thermal insulationPatent ApplicationAttorney Docket No.: 235.0017-WO00 reduces the heat transferred to the plurality of walls via steam, reducing the amount of steam needed for heating the reactor 33 during a steam pressurization step of a steam-assisted TVSA process and improving the efficiency of the steam-assisted TVSA process. In some embodiments of the invention, each reactor 33 is fluidly connected to an air evacuation pump for evacuating air from the vacuum chamber of the reactor 33 when the at least one door 301 is closed. In some embodiments of the invention, each reactor 33 is fluidly connected to drain lines for removing condensate from the reactor 33. The air evacuation pump may be activated when the solid sorbent inside the reactor 33 is to undergo desorption or cooling under vacuum. In some embodiments of the invention, the reactor can exhibit alternative forms, such as that of a moving bed that transfers the solid sorbent between different regions or chambers designated for adsorption and desorption of the solid sorbent.

[0064] FIG. 3 shows another exemplary embodiment of a CCSS of the invention in which air passing out of the plurality of DAC modules is recirculated for improved heat recapture. As in FIG. 2A, the CCSS comprises a heat pump 1, wherein heat pump 1 comprises a refrigerant, a heat pump condenser 2, and a heat pump evaporator 19. In some embodiments of the invention, the heat pump 1 is powered by an electrical input. The CCSS further comprises a steam accumulator 3, a feedwater pump 18, a first storage tank 20, a second storage tank 24, a plurality of DAC modules 6, a first steam condenser 10, a second steam condenser 14, a first separator 11, a second separator 15, and an air-heated heat exchanger 23. Fluid enters the plurality of DAC modules 6 via module inlet valves 5 and exits the plurality of DAC modules 6 via module outlet valves 7. The heat pump condenser 2 is fluidly connected to the steam accumulator 3 and the feedwater pump 18. The heat pump evaporator 19 is fluidly connected to the first storage tank 20 and is fluidly connected to the second storage tank 24 via a second heat transfer fluid pump 25. The first storage tank 20 and the second storage tank 24 serve as repositories and distribution nodes for a heat transfer fluid 21.

[0065] Heat transfer fluid 21 is circulated in a cycle denoted by the counterclockwise flow along the dotted lines in FIG. 3. Heat transfer fluid 21 is stored in the first storage tank 20 as well as the second storage tank 24. The cycle starts by transferring heat transfer fluid 21 from the first storage tank 20 via a first heat transfer fluid pump 22 to the air heated heat exchanger 23. The cycle ends by transferring the heat transfer fluid 21 from the second storage tank 24 and through the heat pump evaporator 19 of heat pump 1 via the second heat transfer fluid pump 25.

[0066] In the exemplary CCSS shown in FIG. 3, the steam accumulator 3 is fluidly connected to at least one of the plurality of DAC modules 6 and is configured to serve as a repository and distribution node for steam 4. The first steam condenser 10 is fluidly connected to at least one of the plurality of DACPatent ApplicationAttorney Docket No.: 235.0017-WO00 modules 6, the second steam condenser 14, the second storage tank 24, and the first separator 11. The second steam condenser 14 is fluidly connected to the first steam condenser 10, the first separator 11, and the second separator 15. The air-heated heat exchanger 23 is fluidly connected to the heat pump 1, and at least one of the first steam condenser 10, and second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the first steam condenser 10 (not shown in FIG. 3). In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is fluidly connected to both the first steam condenser 10 and the second steam condenser 14.

[0067] The exemplary CCSS shown in FIG 3 further comprises a cooling pump 17, which is fluidly connected to at least one of the plurality of DAC modules 6 and the second steam condenser 14. In some embodiments of the invention, the cooling pump 17 is a vacuum pump that evacuates the plurality of DAC modules 6 during a cooling step of the steam-assisted TVSA process.

[0068] The exemplary CCSS shown in FIG. 3 further comprises a vacuum pump 26, which is fluidly connected to at least one of the plurality of DAC modules 6. The vacuum pump 26 extracts air from the plurality of DAC modules 6 during an air evacuation step of the steam-assisted TVSA process as evacuated air 28.

[0069] In the exemplary CCSS of FIG.3, any water that is condensed inside the first steam condenser 10 and the second steam condenser 14 is deposited inside the first separator 11 and the second separator 15, respectively, as condensate 9. Condensate 9 is then pumped from the first separator 11 via a first condensate pump 13 to a condensate tank 8. Similarly, condensate 9 is pumped from the second separator 15 via a second condensate pump 16 to the condensate tank 8. Any water that condenses inside the plurality of DAC modules 6, such as condensate 9, is drained and routed back to the condensate tank 8. Product CO? 1 is extracted from the second separator 15 via a boost blower 12.

[0070] In the exemplary CCSS of FIG. 3, the air-heated heat exchanger 23 is heated not just with ambient air but with the diverted exhaust gas streams 34 from the plurality of DAC modules 6. Under this embodiment, shared ducts, air baffles, pipes, or air-movers direct the exhaust gas streams 34 that exit any of plurality of DAC modules 6 to the air-heated heat exchanger 23 during an adsorption step of a steam-assisted TVSA process. The exhaust gas streams 34, which exhibit conditions near ambient temperature, pressure, and humidity, can be used to transfer heat to a cooler heat transfer fluid 21 passing through the air-heated heat exchanger 23 on the way to condense the steam in the second steam condenser 14.Patent Application Attorney Docket No.: 235.0017-WO00

[0071] FIG. 4 shows another exemplary embodiment of a CCSS of the invention, in which supplemental external heating is provided to the heat transfer circulation loop. As in FIG. 2A, the CCSS comprises a heat pump 1, wherein heat pump 1 comprises a refrigerant, a heat pump condenser 2, and a heat pump evaporator 19. In some embodiments of the invention, the heat pump 1 is powered by an electrical input. The CCSS further comprises a steam accumulator 3, a feedwater pump 18, a first storage tank 20, a second storage tank 24, a plurality of DAC modules 6, a first steam condenser 10, a second steam condenser 14, a first separator 11, a second separator 15, and an air-heated heat exchanger 23. Fluid enters the plurality of DAC modules 6 via module inlet valves 5 and exits the plurality of DAC modules 6 via module outlet valves 7. The heat pump condenser 2 is fluidly connected to the steam accumulator 3 and the feedwater pump 18. The heat pump evaporator 19 is fluidly connected to the first storage tank 20 and is fluidly connected to the second storage tank 24 via a second heat transfer fluid pump 25. The first storage tank 20 and the second storage tank 24 serve as repositories and distribution nodes for a heat transfer fluid 21. The steam accumulator 3 is fluidly connected to at least one of the plurality of DAC modules 6. The steam accumulator 3 is configured to serve as a repository and distribution node for steam 4. The first steam condenser 10 is fluidly connected to at least one of the plurality of DAC modules 6, the second steam condenser 14, the second storage tank 24, and the first separator 11. The second steam condenser 14 is fluidly connected to the first steam condenser 10, the first separator 11, and the second separator 15. The air-heated heat exchanger 23 is fluidly connected to the heat pump 1 and at least one of the first steam condenser 10 and the second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the first steam condenser 10 (not shown in FIG. 4). In some embodiments of the invention, the air-heated heat exchanger 23 is directly connected to the second steam condenser 14. In some embodiments of the invention, the air-heated heat exchanger 23 is fluidly connected to both the first steam condenser 10 and the second steam condenser 14.

[0072] Heat transfer fluid 21 is circulated in a cycle denoted by the counterclockwise flow along the dotted lines in FIG. 4. Heat transfer fluid 21 is stored in the first storage tank 20 as well as the second storage tank 24. The cycle starts by transferring heat transfer fluid 21 from the first storage tank 20 via a first heat transfer fluid pump 22 to the air heated heat exchanger 23. Heat is transferred to the heat transfer fluid 21 inside via the air-heated heat exchanger 23, wherein the air-heated heat exchanger 23 is heated using ambient air 29, either through passive flow or induced flow, such as via fans or blowers. The cycle ends by transferring the heat transfer fluid 21 from the second storage tank 24 and through the heat pump evaporator 19 of heat pump 1 via the second heat transfer fluid pump 25.Patent ApplicationAttorney Docket No.: 235.0017-WO00

[0073] The exemplary CCSS shown in FIG 4 further comprises a cooling pump 17, which is fluidly connected to at least one of the plurality of DAC modules 6 and the second steam condenser 14. In some embodiments of the invention, the cooling pump 17 is a vacuum pump that evacuates the plurality of DAC modules 6 during a cooling step of the steam-assisted TVSA process.

[0074] The exemplary CCSS shown in FIG. 4 further comprises a vacuum pump 26, which is fluidly connected to at least one of the plurality of DAC modules 6. The vacuum pump 26 extracts air from the plurality of DAC modules 6 during an air evacuation step of the steam-assisted TVSA process as evacuated air 28.

[0075] In the exemplary CCSS of FIG. 4, any water that is condensed inside the first steam condenser 10 and the second steam condenser 14 is deposited inside the first separator 11 and the second separator 15, respectively, as condensate 9. Condensate 9 is then pumped from the first separator 11 via a first condensate pump 13 to a condensate tank 8. Similarly, condensate 9 is pumped from the second separator 15 via a second condensate pump 16 to the condensate tank 8. Any water that condenses inside the plurality of DAC modules 6, such as condensate 9, is drained and routed back to the condensate tank 8. Product CO21 is extracted from the second separator 15 via a boost blower 12.

[0076] In the exemplary CCSS of FIG. 4, an auxiliary heat source 36 is added to the heat transfer fluid 21 loop of the CCSS. In some embodiments of the invention, the auxiliary heat source 36 is fluidly connected between the second storage tank 24 and the first steam condenser 10. In some embodiments of the invention, the auxiliary heat source 36 is an electric heater, a resistive heater, or a boiler. In some embodiments of the invention, the auxiliary heat source uses electric power to further warm the heat transfer fluid 21 when ambient conditions (such as freezing weather or cold climates) cannot reliably provide sufficient heat for the heat transfer fluid 21 to boil water into steam via heat pump 1.

[0077] FIG. 5 shows an exemplary embodiment of a CCSS of the invention, in which a vapor recompressor is incorporated into the steam and water recirculation loop. As in FIG. 2A, the CCSS comprises a heat pump 1, wherein heat pump 1 comprises a refrigerant, a heat pump condenser 2, and a heat pump evaporator 19. In some embodiments of the invention, the heat pump 1 is powered by an electrical input and comprises a mechanical compressor (not shown) for increasing the pressure of the refrigerant and an expansion valve (not shown) for decreasing the pressure of the refrigerant.

[0078] In the exemplary embodiment of FIG. 5, the CCSS further comprises a feedwater pump 18, a first storage tank 20, a second storage tank 24, a plurality of DAC modules 6, a first steam condenser 10, a first separator 11, and an air-heated heat exchanger 23. Fluid enters the plurality of DAC modules 6 via module inlet valves 5 and exits the plurality of DAC modules 6 via module outlet valves 7. The heatPatent Application Attorney Docket No.: 235.0017-WO00 pump condenser 2 is fluidly connected the feedwater pump 18. The heat pump evaporator 19 is fluidly connected to the first storage tank 20 and is fluidly connected to the second storage tank 24 via a second heat transfer fluid pump 25. The first storage tank 20 and the second storage tank 24 serve as repositories and distribution nodes for a heat transfer fluid 21. The first steam condenser 10 is fluidly connected to at least one of the plurality of DAC modules 6, steam accumulator 3, and the first separator 11. The air-heated heat exchanger 23 is fluidly connected to the heat pump 1, first storage tank 20, and second storage tank 24. Unlike in FIG. 2A, there is no steam accumulator between the heat pump 1 and the plurality of DAC modules 6. Instead, the steam accumulator 3 is fluidly connected to at least one of the plurality of DAC modules 6, the feedwater pump 18, and the first steam condenser 10 and is configured to serve as a repository and distribution node for steam 4.

[0079] The exemplary CCSS shown in FIG. 5 further comprises a vacuum pump 26, which is fluidly connected to at least one of the plurality of DAC modules 6. The vacuum pump 26 extracts air from the plurality of DAC modules 6 during an air evacuation step of the steam-assisted TVSA process as evacuated air 28.

[0080] Heat transfer fluid 21 is circulated in a cycle denoted by the counterclockwise flow along the dotted lines in FIG. 5. Heat transfer fluid 21 is stored in the first storage tank 20 as well as the second storage tank 24. The cycle starts by transferring the heat transfer fluid 21 from the first storage tank 20 via a first heat transfer fluid pump 22 to the air heated heat exchanger 23. Heat is transferred to the heat transfer fluid 21 inside via the air-heated heat exchanger 23, wherein the air-heated heat exchanger 23 is heated using ambient air 29, either through passive flow or induced flow, such as via fans or blowers. The cycle ends by transferring the heat transfer fluid 21 from the second storage tank 24 and through the heat pump evaporator 19 of heat pump 1 via the second heat transfer fluid pump 25.

[0081] In the exemplary CCSS of FIG. 5, any water that is condensed inside the first steam condenser 10 is deposited inside the first separator 11 as condensate 9. Condensate 9 is pumped from the first separator 11 via a first condensate pump 13 back through the first steam condenser 10 and to steam accumulator 3, which can comprise a mixture of steam 4 and condensate 9. The condensate 9 may settle to the bottom of the accumulator and the steam 4 may rise to the top of the accumulator. Any water that condenses inside the plurality of DAC modules 6, such as condensate 9, is also drained and routed to steam accumulator 3. Condensate 9 can be mixed with makeup water source 37 and supplied to heat pump 1 to make new steam 4. Steam 4 in steam accumulator 3 is supplied to at least one of the pluralityPatent Application Attorney Docket No.: 235.0017-WO00 of DAC modules 6. Product CO21 is ultimately extracted from the first separator 11 via a boost blower12.

[0082] In the exemplary CCSS of FIG. 5, an auxiliary heat source 36 is added to the CCSS in the heat transfer fluid 21 loop. In some embodiments of the invention, the auxiliary heat source 36 is fluidly connected between the second storage tank 24 and the air-heated heat exchanger 23. In some embodiments of the invention, the auxiliary heat source 36 is an electric heater, a resistive heater, or a boiler. In some embodiments of the invention, the auxiliary heat source uses electric power to further warm the heat transfer fluid 21 when ambient conditions (such as freezing weather or cold climates) cannot reliably provide sufficient heat for the heat transfer fluid 21 to boil water into steam via heat pump 1.

[0083] In the exemplary embodiment of FIG. 5, a vapor re-compressor 38 is fluidly connected to a cooling pump 17, at least one of the plurality of DAC modules 6, and the steam condenser 10. The vapor re-compressor 38 takes in as an input the mixture of steam and CO2that exits the plurality of DAC modules 6 via the module output valves 7 after a steam purging or cooling step of a steam-assisted TVSA process. In some embodiments of the invention, the mixture of steam and CO2exits the plurality of DAC modules 6 through a second module output valve (shown in FIG. 2B). In some embodiments of the invention, the mixture of steam and CO2exits the plurality of DAC modules 6 through a third module output valve (shown in FIG. 2B). The vapor re-compressor 38 recovers heat from water vapor output by the at least one reactor contained within each of the plurality of DAC modules 6 by compressing it, thereby heating condensate back into steam and augmenting the recuperative heat exchange function of the first steam condenser 10. This allows for steam to be circulated back to the steam accumulator 3, which supplements the steam generated by the heat pump 1. The exemplary CCSS of FIG. 5 further comprises makeup water source 37, which is fluidly connected to the steam accumulator 3. Makeup water source 37 can come from treated water systems or other water repositories or utilities and can be used to refill the balance of water in the steam accumulator 3. Any water collected at the bottom of the steam accumulator 3 is pumped to the heat pump 1 via the feedwater pump 18 to supply additional water for steam generation.

[0084] FIG. 6 shows an exemplary CCSS of the invention, in which a plurality of heat pumps deliver heat to the process streams feeding a plurality of DAC modules 6. A plurality of heat pumps 1 deliver steam to unique subsets of a plurality of DAC modules 6, wherein each subset comprises at least one DAC module and each of the at least one DAC module comprises at least one reactor. Each of the plurality of heat pumps 1 receives heat from a heat transfer fluid 21 that undergoes a thermal cycle 40. An airPatent ApplicationAttorney Docket No.: 235.0017-WO00 heated heat exchanger 23 delivers heat to the heat transfer fluid 21 from ambient air as part of the thermal cycle 40. The plurality of DAC modules 6 may all drain condensate 9 to a common condensate tank 8. The at least one reactor contained within each of the plurality of DAC modules 6 may all be evacuated by a common pump system 41 which outputs exhaust air 28. The plurality of DAC modules 6 may deliver a product stream comprising a mixture of CO2, condensate, and steam to a separator system 42, which separates the product stream into CO227 and condensate 9. Condensate 9 can be drawn from the separator system 42 to the condensate tank 8, while CO227 can be drawn from the separator system 42 to an industrial application or carbon sequestration facility via blower or pump 43.

[0085] Benefits of the CCSS of the invention are evident when the ratio of energy output from the airheated heat pump (in the form of heat) to energy input (in the form of work) is calculated. This ratio is also known in the art of heat pumps and refrigeration systems as the Coefficient of Performance (COP) for heating. A heating system that supplies the same amount of heat using ideal resistance heating without heat pumps has an effective coefficient of performance (CO Perfective) for heating of one. When using a heat pump system in accordance with the invention, the CO Peffective is greater than 1, such as for example, having a COPeffective of between 1 and 5, inclusive. This means that the same amount of heat can be supplied by the system with less energy input by taking advantage of the latent heat in ambient air. The COPeffective of the present heat pump system ultimately depends on many factors, including the thermodynamic and transport properties of the heat transfer fluid, the isentropic efficiencies of the compressors, the size of the air-heated heat exchanger, the temperature required for CO2desorption, the temperature required to cool the sorbent prior to resuming adsorption, and the average ambient air temperature where the system is located.

[0086] The invention further relates to a method of capturing CO2having an improved COPeffective as shown in FIG. 8. The disclosed method comprises a sequence of steps performed in a repetitive carbon capture cycle for each of the at least one reactor within each of at least one DAC module. The number of reactors undertaking any step of the cycle may be proportional to the fraction of the total cycle time a single reactor spends undertaking each step. For example, if 70% of the cycle time is spent in Step 1, then at any single moment in time the same number of reactors (i.e., 70% of all reactors) may be operating in Step 1. Each reactor undergoes the disclosed sequence of steps in the same order, but as previously disclosed not all reactors undergo the same step simultaneously. Individual reactors may be selected to operate in each step of the cycle by opening and closing valves located inside each of the at least one DAC module to control the inlet and outlet flow of a plurality of fluid streams.Patent ApplicationAttorney Docket No.: 235.0017-WO00

[0087] The invention further relates to a method for capturing CO2 through a steam-assisted TVSA process comprising an adsorption step, an air evacuation step, a steam pressurization step, a steam purging step, a cooling step, and an air pressurization step. This method can be carried out by a CCSS of the invention, including any of the exemplary CCSSs of FIGS. 2A, 3, 4, 5, and 6.

[0088] Step 1: Adsorption

[0089] In an adsorption step of a steam-assisted TVSA process of the invention, ambient air, which is air exhibiting ambient temperature and ambient humidity such as having a temperature between 20° C and 25° C and a pressure between 0.9 and 1.1 bar, is directed through a reactor housing a solid sorbent that is contained inside a DAC module and across the solid sorbent. The solid sorbent adsorbs CO2from the ambient air that passes across it. The ambient air is passed over the solid sorbent via forced convection, passive exposure, or naturally occurring wind. During the adsorption step, the flow of ambient air cools the solid sorbent to (or nearly to-) the temperature of the ambient air.

[0090] In an alternative embodiment of the invention, the adsorption step further comprises redirecting at least a portion of the ambient air exiting the reactor to an air-heated heat exchanger through which flows a heat transfer fluid. The ambient air that exits the reactor warms the heat transfer fluid inside the air-heated heat exchanger. In some embodiments of the invention, the heat transfer fluid is warmed inside the air-heated heat exchanger to a temperature between 25° C and 30° C.

[0091] Step 2: Air Evacuation

[0092] In an air evacuation step of the steam-assisted TVSA process of the invention, an air evacuation pump evacuates the air from the reactor. In some embodiments of the invention, the air evacuation pump depressurizes the reactor to a pressure between 10 mbar and 300 mbar. In a preferred embodiment of the invention, the air evacuation pump depressurizes the reactor to a pressure less than or equal to 60 mbar. The removal of air from the reactor ameliorates the risk of damaging the solid sorbent housed therein via oxidation (the solid sorbent can oxidize at higher temperatures and is heated in the steam pressurization step laid out below). Evacuating air from the reactor prior to desorption of CO2 from the solid sorbent removes impurity elements from the final CO2product, and the CCSS thereby outputs a product gas that is substantially pure CO2.

[0093] In an alternative embodiment of the invention, the air evacuation step further comprises directing evacuated air withdrawn from the reactor via the air evacuation pump to the air-heated heat exchanger through which flows the heat transfer fluid. The evacuated air from the reactor warms the heat transfer fluid inside the air-heated heat exchanger. In some embodiments of the invention, the heat transfer fluid is warmed inside the air-heated heat exchanger to a temperature between 25° C andPatent ApplicationAttorney Docket No.: 235.0017-WO0030° C.

[0094] Step 3: Steam Pressurization

[0095] In a steam pressurization step of the steam-assisted TVSA process of the invention, steam is directed from a steam accumulator into the reactor, wherein the steam directly contacts the solid sorbent housed therein and heats the solid sorbent. In some embodiments of the invention, the steam heats the solid sorbent to a temperature between 50° and 110° C. In a preferred embodiment, the steam heats the solid sorbent to a temperature between 80° and 100° C. The ingress of steam also pressurizes the reactor. When heated, the solid sorbent desorbs CO2inside the pressurized reactor to create a product mixture of steam and CO2. A significant portion of the steam is adsorbed in the sorbent material of the solid sorbent, and the heat released during the adsorption step also heats the solid sorbent. Steam that is not adsorbed by the solid sorbent condenses inside the reactor and is drained via gravity from the reactor and the DAC module containing the reactor to a condensate tank.

[0096] Step 4: Steam Purging

[0097] In a steam purging step of the steam-assisted TVSA process of the invention, steam is directed through the reactor within the DAC module to purge CO2gas that was desorbed from the solid sorbent during the steam pressurization step. The resulting product mixture of steam and CO2is directed to at least one steam condenser (e.g., a first steam condenser), wherein steam is condensed into liquid water and the product mixture becomes a mixture of steam, water, and CO2. Condensate and CO2are separated downstream of the at least one steam condenser in at least one separator (e.g., a first separator). Condensate is pumped from the at least one separator to a condensate tank by way of a motive force of at least one condensate pump (e.g., a first condensate pump).

[0098] In an alternative embodiment of the invention, the heat of condensation of the steam is transferred to the heat transfer fluid via at least one steam condenser. This raises the temperature of the heat transfer fluid higher than the temperature it reached via the air-heated heat exchanger. In this manner, at least one steam condenser present in the heat transfer fluid loop can utilize the heat of condensation generated as part of the separation of the product gas drawn from the at least one DAC module to pre-heat the heat transfer fluid prior to its transfer to the heat pump. In some embodiments of the invention, the at least one steam condenser raises the temperature of the heat transfer fluid to between 50° C and 95° C.

[0099] In an alternative embodiment of the invention, the product mixture of steam and CO2is subsequently directed into a first steam condenser and then into a second steam condenser. A first steam condenser condenses a first portion of steam into liquid water. The second steam condenserPatent ApplicationAttorney Docket No.: 235.0017-WO00 condenses a second portion of steam into liquid water. The heat of condensation of steam is also transferred to the heat transfer fluid via the first and second steam condensers. The first steam condenser may be configured to warm the heat transfer fluid to a first intermediate temperature, such as between 40° C and 60° C, and the second steam condenser may be configured to further warm the heat transfer fluid to a second intermediate temperature, such as between 50° C and 95° C, that is higher than the first intermediate temperature. In this manner, the combination of multiple steam condensers present in the heat transfer fluid loop can utilize the heat of condensation generated as part of the separation of the product gas drawn from the at least one DAC module to pre-heat the heat transfer fluid prior to its transfer to the heat pump.

[0100] Step 5: Cooling

[0101] In a cooling step of the steam-assisted TVSA process of the invention, a cooling pump evacuates air from the reactor. In some embodiments of the invention, the cooling pump depressurizes the reactor to a pressure less than or equal to 400 mbar. In a preferred embodiment of the invention, the cooling pump depressurizes the reactor to a pressure less than or equal to 150 mbar. Lowering the pressure of the reactor cools the solid sorbent housed therein, and the desorption of water vapor and the remaining CO2 further cools the solid sorbent by virtue of the released heat of desorption. The cooling pump is continuously operated until the solid sorbent reaches a temperature less than or equal to 60°C. Evacuated water vapor is diverted to at least one steam condenser, wherein the water vapor is condensed. The condensed water from the at least one steam condenser is separated from the CO2in at least one separator. After leaving the cooling pump, the mixture of CO2and water vapor is further cooled and condensed in the at least one steam condenser. The transfer of heat from the heat transfer fluid vaporizes the refrigerant in the heat pump evaporator. The colder liquid in a storage tank is pumped through the air-heated heat exchanger and the at least one steam condenser via the motive force of a heat transfer fluid pump before returning as a hotter liquid to a storage tank.

[0102] In some embodiments of the invention, the refrigerant is a heat transfer medium in gas or liquid phase such as a hydrocarbon, a hydrofluoroolefin, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, ammonia, or a mixture of water and glycol.

[0103] In some embodiments of the invention, the heat of condensation is transferred to the heat transfer fluid via the at least one steam condenser.

[0104] In some embodiments of the invention, the heat transfer fluid is circulated between two storage tanks in fluid connection with the heat pump and the air-heated heat exchanger.

[0105] In some embodiments of the invention, the product mixture of steam and CO2is subsequentlyPatent ApplicationAttorney Docket No.: 235.0017-WO00 directed into first and second steam condenser. A first steam condenser condenses a first portion of steam into liquid water. The second steam condenser condenses a second portion of steam into liquid water. Evacuated water vapor is the second steam condenser, wherein the water vapor is condensed. The condensed water from the at least one steam condenser is separated from the CO2 in second separator. After leaving the cooling pump, the mixture of CO2and water vapor is further cooled and condensed in the second steam condenser. The transfer of heat from the heat transfer fluid vaporizes the refrigerant in the heat pump evaporator. The colder liquid in the second storage tank is pumped through the air-heated heat exchanger, the first steam condenser, and the second steam condenser via the motive force of the second heat transfer fluid pump before returning as a hotter liquid to the first storage tank.

[0106] Step 6: Air Pressurization

[0107] In an air pressurization step of the steam-assisted TVSA process of the invention, an air outlet valve of the cooled reactor is opened to equalize the pressure of the reactor with atmospheric pressure. The air outlet valve is opened gradually to prevent a rapid inrush of air from potentially damaging the solid sorbent housed within the reactor.

[0108] The above method for capturing CO2 can then repeat for the reactor, starting with Step 1. Output product stream of CO2 is extracted from the second separator using a boost blower where it can be further utilized or sequestered. The recovered product CO2is delivered at a pressure slightly above atmospheric pressure by way of the motive force of the boost blower. In some embodiments of the invention, the boost blower is a fan that can overcome a pressure drop greater than 0.1 bar (or 100 mbar).

[0109] In an alternative method of capturing CO2of the invention, an additional heating step is carried out. An auxiliary heat source fluidly connected between the second storage tank and the first steam condenser is utilized to warm the heat transfer fluid when ambient conditions cannot efficiently run the heat pump. The auxiliary heat source may be an electric heater, a boiler, or other suitable heating element.

[0110] The invention further relates to a method of capturing CO2 comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air; delivering heat to a heat transfer fluid using a heat exchanger, wherein the heat exchanger delivers heat from ambient air to the heat transfer fluid; generating steam using at least one heat pump, wherein the at least one heat pump acceptsPatent ApplicationAttorney Docket No.: 235.0017-WO00 heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the solid sorbent in the at least one evacuated reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

[0111] The invention further relates to a method of capturing CO2comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air, and wherein the ambient air exits the at least one reactor as exhaust after making contact with the at least one solid sorbent; directing a portion of the exhaust to a heat exchanger through which flows a heat transfer fluid, wherein the portion of exhaust warms the heat transfer fluid inside the heat exchanger; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the at least one solid sorbent in the at least one reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2inside the at least one reactor to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; andPatent ApplicationAttorney Docket No.: 235.0017-WO00 directing the CO? to a product stream.

[0112] In some embodiments of the invention, the steam generated by the at least one heat pump exhibits a pressure of at least 1.0 bar and a temperature of at least 100° C.

[0113] In some embodiments of the invention, the method steps are repeated and staggered using a plurality of subsets of reactors, and wherein one subset of reactors simultaneously undergoes a different step than another subset of reactors. In some embodiments of the invention, a subset of reactors undergoes the step of directing ambient air through the at least one reactor containing the at least one solid sorbent while another subset of reactors undergoes the step of heating the at least one solid sorbent to a temperature between 80° and 100° C.

[0114] In some embodiments of the invention, the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume. In some embodiments of the invention, the at least one solid sorbent is one of a zeolite or amine-functionalized compound, such as amine-functionalized siliceous, inorganic, activated carbon, graphitic, metal organic framework (MOF) or polymeric compounds. In some embodiments of the invention, the at least one solid sorbent is amine-functionalized carbon, glass, cellulosic, or polymeric fibers. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine impregnated onto a porous support such as silica, alumina, or activated carbon. In some embodiments of the invention, the at least one solid sorbent is an amine or polyamine grafted onto a porous support such as silica, alumina, or mesoporous materials like SBA-15 or MCM-41. In some embodiments of the invention, the at least one solid sorbent is a basic or weakly basic ion exchange resin. In some embodiments of the invention, the at least one solid sorbent is a MOF, a porous organic polymer, a covalent organic framework (COF), a porous aromatic framework (PAF), or a hypercrosslinked polymer. In some embodiments of the invention, the at least one solid sorbent is formed as a powder, pellet, fluidized bed, packed bed, fibrous web, fibrous mat, woven fabric, structured monolith, sheet, film, membrane, or plate. In some embodiments of the invention, the at least one solid sorbent is containerized within a support cartridge to form parallel-plate structures or vertical stacks.

[0115] The CCSS of the invention is scalable for a large number of DAC modules and constituent reactors. The sizes and outputs of the heat pump and the volume of the fluid storage tanks scale accordingly with the quantity of reactors and DAC modules.

[0116] The foregoing detailed description of the certain exemplary embodiments has been provided for the purpose of explaining the principles of the invention and its practical application, thereby enabling others skilled in the art to understand the invention for various embodiments and with variousPatent ApplicationAttorney Docket No.: 235.0017-WO00 modifications as are suited to the particular use contemplated. This description is not necessarily intended to be exhaustive or to limit the invention to the precise embodiments disclosed. The specification describes specific examples of accomplishing a more general goal that also may be accomplished in another way. Those skilled in the art will appreciate that the features described above can be combined in various ways to form multiple variations of the invention. All of the references cited herein are incorporated by reference herein for all purposes, or at least for their teachings in the context presented.

[0117] Exemplary Embodiments of the Invention

[0118] El. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (CO2) from the atmosphere, the CCSS comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2from the air and desorbing CO2into a product stream; a piping network; a heat pump; a process stream comprising water and disposed in the piping network, wherein the heat pump delivers heat to the process stream to generate steam; a heat transfer fluid disposed in the piping network, wherein the heat pump receives heat from the heat transfer fluid; at least one storage tank for storing heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger delivers heat to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump fluidly connected to the at least one condensate tank for delivering water from the at least one condensate tank to the process stream.

[0119] E2. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (CO2) from the atmosphere, the CCSS comprising:Patent ApplicationAttorney Docket No.: 235.0017-WO00 at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2 from the air and desorbing CO2 into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump fluidly connected to the at least one DAC module, wherein the heat pump is configured to generate steam, and wherein the heat pump comprises: a refrigerant; an expansion valve for reducing a pressure of the refrigerant; a compressor for increasing the pressure of the refrigerant; an evaporator for vaporizing the refrigerant; and a heat pump condenser disposed in the piping network configured to transfer heat from the refrigerant to a process stream comprising water, wherein the heat pump is fluidly connected to the at least one DAC module via the piping network; a heat transfer fluid disposed in the piping network, wherein the evaporator receives heat from the heat transfer fluid; at least one storage tank for storing the heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one cooling pump fluidly connected to the at least one DAC module that acts to cool the at least one solid sorbent; at least one air evacuation pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2 and water; at least one condenser fluidly connected to the at least one DAC module, wherein the at least one condenser condenses steam into condensate; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger transfers heat from ambient air to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump for delivering water from the at least one condensate tank to the process stream.

[0120] E3. The CCSS of El or E2, further comprising an auxiliary heat source, wherein: the auxiliary heat source is disposed in the piping network between the at least one condenserPatent ApplicationAttorney Docket No.: 235.0017-WO00 and the heat pump, the auxiliary heat source is fluidly connected to the at least one condenser and the at least one storage tank that stores the heat transfer fluid, and the auxiliary heat source warms the heat transfer fluid before it flows to the at least one storage tank and the heat pump.

[0121] E4. The CCSS of El, further comprising a vapor re-compressor, wherein: the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one pump, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one pump, and the at least one DAC module, and the vapor re-compressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

[0122] E5. The CCSS of E2, further comprising a vapor re-compressor, wherein: the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one cooling pump, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one cooling pump, and the at least one DAC module, and the vapor re-compressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

[0123] E6. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (CO2) from the atmosphere, the system comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2 from the air and desorbing CO2 into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump comprising a heat pump evaporator and a heat pump condenser, wherein the heat pump is fluidly connected to a steam accumulator and the at least one DAC module via the piping network, wherein the heat pump condenser outputs condensed water to the steam accumulator as steam, and wherein the heat pump condenser outputs a heat transfer fluid to the at least one DAC module; the heat transfer fluid disposed in the piping network, wherein the heat transfer fluid flows through the heat pump evaporator and delivers heat to the heat pump;Patent ApplicationAttorney Docket No.: 235.0017-WO00 at least one auxiliary steam condenser fluidly connected to the at least one DAC module, wherein the at least one DAC module outputs a mixture of steam and CO2to the at least one auxiliary steam condenser; at least one separator fluidly connected to the at least one auxiliary steam condenser, wherein the at least one separator separates the product stream into CO2and water; and an air-heated heat exchanger fluidly connected to the heat pump and the at least one auxiliary steam condenser, wherein: the air-heated heat exchanger is heated using exhaust air output from the at least one DAC module; the heat transfer fluid flows through the air-heated heat exchanger via the piping network; and the air-heated heat exchanger delivers heat to the heat transfer fluid.

[0124] E7. The CCSS of any one of E1-E6, further comprising a plurality of heat pumps, wherein each of the plurality of heat pumps is fluidly connected to a unique set of the at least one DAC module via the piping network.

[0125] E8. The CCSS of any one of E1-E6, wherein the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume.

[0126] E9. The CCSS of any one of E1-E6, wherein each of the at least one DAC module comprises a plurality of the at least one reactor, wherein each of the plurality of the at least one reactor comprises an enclosed cavity that houses the at least one solid sorbent, and wherein each of the plurality of the at least one reactor can be independently opened or closed for the respective adsorption and desorption of CO2by the at least one solid sorbent.

[0127] E10. The CCSS of any one of E1-E6, wherein the at least one solid sorbent is a zeolite or amine- functionalized compound.

[0128] Ell. The CCSS of El or E2, further comprising a steam accumulator fluidly connected to the heat pump and the at least one DAC module, wherein steam that exits the heat pump flows into the steam accumulator and steam from the steam accumulator flows into the at least one DAC module.

[0129] E12. The CCSS of Ell, wherein the delivery of steam from the steam accumulator to the at least one DAC module is dynamically adjusted depending on the number of the at least one DAC module or at least one reactor which are opened or closed for the respective adsorption and desorption of CO2by the at least one solid sorbent.

[0130] E13. A method of capturing carbon dioxide (CO2), comprising the steps of:Patent ApplicationAttorney Docket No.: 235.0017-WO00 directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air; delivering heat to a heat transfer fluid using a heat exchanger, wherein the heat exchanger delivers heat from ambient air to the heat transfer fluid; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the solid sorbent in the at least one evacuated reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

[0131] E14. A method of capturing carbon dioxide (CO2), comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air, and wherein the ambient air exits the at least one reactor as exhaust after making contact with the at least one solid sorbent; directing a portion of the exhaust to a heat exchanger through which flows a heat transfer fluid, wherein the portion of exhaust warms the heat transfer fluid inside the heat exchanger; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the at least one solid sorbent in the at least one reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2inside the at least one reactor to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least onePatent ApplicationAttorney Docket No.: 235.0017-WO00 condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO? in at least one separator; directing the condensate to a condensate tank; and directing the CO? to a product stream.

[0132] E15. The method of capturing CO? of E13 or E14, wherein the steam generated by the at least one heat pump exhibits a pressure of at least 1.0 bar and a temperature of at least 100° C.

[0133] E16. The method of capturing CO? of any one of E13-E15, wherein the method steps are repeated and staggered using a plurality of subsets of reactors, and wherein one subset of reactors simultaneously undergoes a different step than another subset of reactors.

[0134] E17. The method of capturing CO2of E16, wherein a subset of reactors undergoes the step of directing ambient air through the at least one reactor containing the at least one solid sorbent while another subset of reactors undergoes the step of heating the at least one solid sorbent to a temperature between 80° and 100° C.

[0135] E18. The method of capturing CO? of any one of E13-E17, wherein the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume.

[0136] E19. The method of capturing CO2of any one of E13-E18, wherein the at least one solid sorbent is a zeolite or amine-functionalized compound.

[0137] E20. The method of capturing CO? of any one of E13-E18, wherein the at least one solid sorbent is a basic or weakly basic ion exchange resin.

[0138] E21. The method of capturing CO2of any one of E13-E18, wherein the at least one solid sorbent is a metal organic framework (MOF), a porous organic polymer, a covalent organic framework (COF), a porous aromatic framework (PAF), or a hypercrosslinked polymer.

[0139] E22. The method of capturing CO2of any one of E13-E18, wherein the at least one solid sorbent is an amine-functionalized siliceous, inorganic, activated carbon, graphitic, metal organic framework (MOF) or polymeric compound.

[0140] E23. The CCSS of any one of E1-E12, wherein the at least one solid sorbent is a basic or weakly basic ion exchange resin.

[0141] E24. The CCSS of any one of E1-E12, wherein the at least one solid sorbent is a metal organic framework (MOF), a porous organic polymer, a covalent organic framework (COF), a porous aromatic framework (PAF), or a hypercrosslinked polymer.Patent ApplicationAttorney Docket No.: 235.0017-WO00

[0142] E25. The CCSS of any one of E1-E12, wherein the at least one solid sorbent is an amine- functionalized siliceous, inorganic, activated carbon, graphitic, metal organic framework (MOF) or polymeric compound.

Claims

Patent ApplicationAttorney Docket No.: 235.0017-WO00What is claimed is:

1. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (COa) from the atmosphere, the CCSS comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2 from the air and desorbing CO2 into a product stream; a piping network; a heat pump; a process stream comprising water and disposed in the piping network, wherein the heat pump delivers heat to the process stream to generate steam; a heat transfer fluid disposed in the piping network, wherein the heat pump receives heat from the heat transfer fluid; at least one storage tank for storing heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger delivers heat to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump fluidly connected to the at least one condensate tank for delivering water from the at least one condensate tank to the process stream.

2. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (CO2) from the atmosphere, the CCSS comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2 from the air and desorbing CO2 into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump fluidly connected to the at least one DAC module, wherein the heat pump isPatent ApplicationAttorney Docket No.: 235.0017-WO00 configured to generate steam, and wherein the heat pump comprises: a refrigerant; an expansion valve for reducing a pressure of the refrigerant; a compressor for increasing the pressure of the refrigerant; an evaporator for vaporizing the refrigerant; and a heat pump condenser disposed in the piping network configured to transfer heat from the refrigerant to a process stream comprising water, wherein the heat pump is fluidly connected to the at least one DAC module via the piping network; a heat transfer fluid disposed in the piping network, wherein the evaporator receives heat from the heat transfer fluid; at least one storage tank for storing the heat transfer fluid, wherein the at least one storage tank is fluidly connected to the heat pump; at least one cooling pump fluidly connected to the at least one DAC module that acts to cool the at least one solid sorbent; at least one air evacuation pump fluidly connected to the at least one DAC module; at least one separator fluidly connected to the at least one DAC module, wherein the at least one separator separates the product stream into CO2and water; at least one condenser fluidly connected to the at least one DAC module, wherein the at least one condenser condenses steam into condensate; a heat exchanger fluidly connected to the heat pump and the at least one condenser, wherein the heat exchanger transfers heat from ambient air to the heat transfer fluid; at least one condensate tank comprising water; and a feedwater pump for delivering water from the at least one condensate tank to the process stream.

3. The CCSS of claim 1 or 2, further comprising an auxiliary heat source, wherein: the auxiliary heat source is disposed in the piping network between the at least one condenser and the heat pump, the auxiliary heat source is fluidly connected to the at least one condenser and the at least one storage tank that stores the heat transfer fluid, and the auxiliary heat source warms the heat transfer fluid before it flows to the at least one storagePatent ApplicationAttorney Docket No.: 235.0017-WO00 tank and the heat pump.

4. The CCSS of claim 1, further comprising a vapor re-compressor, wherein: the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one pump, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one pump, and the at least one DAC module, and the vapor re-compressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

5. The CCSS of claim 2, further comprising a vapor re-compressor, wherein: the vapor re-compressor is disposed in the piping network between the at least one condenser and the at least one cooling pump, the vapor re-compressor is fluidly connected to the at least one condenser, the at least one cooling pump, and the at least one DAC module, and the vapor re-compressor recovers heat from the product stream by compressing the product stream and converting the condensate back into steam.

6. A carbon dioxide capture and separation system (CCSS) for removing carbon dioxide (CO2) from the atmosphere, the system comprising: at least one direct air capture (DAC) module, wherein each of the at least one DAC module comprises at least one reactor, and wherein each of the at least one reactor comprises at least one solid sorbent capable of adsorbing CO2 from the air and desorbing CO2 into a product stream; a piping network comprising a plurality of pipes and valves; a heat pump comprising a heat pump evaporator and a heat pump condenser, wherein the heat pump is fluidly connected to a steam accumulator and the at least one DAC module via the piping network, wherein the heat pump condenser outputs condensed water to the steam accumulator as steam, and wherein the heat pump condenser outputs a heat transfer fluid to the at least one DAC module; the heat transfer fluid disposed in the piping network, wherein the heat transfer fluid flows through the heat pump evaporator and delivers heat to the heat pump; at least one auxiliary steam condenser fluidly connected to the at least one DAC module,Patent ApplicationAttorney Docket No.: 235.0017-WO00 wherein the at least one DAC module outputs a mixture of steam and CO? to the at least one auxiliary steam condenser; at least one separator fluidly connected to the at least one auxiliary steam condenser, wherein the at least one separator separates the product stream into CO? and water; and an air-heated heat exchanger fluidly connected to the heat pump and the at least one auxiliary steam condenser, wherein: the air-heated heat exchanger is heated using exhaust air output from the at least one DAC module; the heat transfer fluid flows through the air-heated heat exchanger via the piping network; and the air-heated heat exchanger delivers heat to the heat transfer fluid.

7. The CCSS of any one of claims 1, 2, or 6, further comprising a plurality of heat pumps, wherein each of the plurality of heat pumps is fluidly connected to a unique set of the at least one DAC module via the piping network.

8. The CCSS of any one of claims 1, 2, or 6, wherein the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume.

9. The CCSS of any one of claims 1, 2, or 6, wherein each of the at least one DAC module comprises a plurality of the at least one reactor, wherein each of the plurality of the at least one reactor comprises an enclosed cavity that houses the at least one solid sorbent, and wherein each of the plurality of the at least one reactor can be independently opened or closed for the respective adsorption and desorption of CO? by the at least one solid sorbent.

10. The CCSS of any one of claims 1, 2, or 6, wherein the at least one solid sorbent is a zeolite or amine-functionalized compound.

11. The CCSS of claim 1 or 2, further comprising a steam accumulator fluidly connected to the heat pump and the at least one DAC module, wherein steam that exits the heat pump flows into the steam accumulator and steam from the steam accumulator flows into the at least one DAC module.Patent Application Attorney Docket No.: 235.0017-WO0012. The CCSS of claim 11, wherein the delivery of steam from the steam accumulator to the at least one DAC module is dynamically adjusted depending on the number of the at least one DAC module or at least one reactor which are opened or closed for the respective adsorption and desorption of CO2by the at least one solid sorbent.

13. A method of capturing carbon dioxide (CO2), comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air; delivering heat to a heat transfer fluid using a heat exchanger, wherein the heat exchanger delivers heat from ambient air to the heat transfer fluid; generating steam using at least one heat pump, wherein the at least one heat pump accepts heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the solid sorbent in the at least one evacuated reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2 to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

14. A method of capturing carbon dioxide (CO2), comprising the steps of: directing ambient air through at least one reactor containing at least one solid sorbent, wherein the at least one solid sorbent adsorbs CO2from the ambient air, and wherein the ambient air exits the at least one reactor as exhaust after making contact with the at least one solid sorbent; directing a portion of the exhaust to a heat exchanger through which flows a heat transfer fluid, wherein the portion of exhaust warms the heat transfer fluid inside the heat exchanger; generating steam using at least one heat pump, wherein the at least one heat pump acceptsPatent ApplicationAttorney Docket No.: 235.0017-WO00 heat from the heat transfer fluid; evacuating the at least one reactor to a pressure of at least 60 mbar or less; directing steam from the at least one heat pump into the at least one evacuated reactor; heating the at least one solid sorbent in the at least one reactor to a temperature between 80° and 100° C, wherein the at least one solid sorbent desorbs CO2inside the at least one reactor to create a product mixture of steam and CO2; directing the product mixture of steam and CO2from the at least one reactor to at least one condenser, wherein the at least one condenser condenses steam into condensate; evacuating the at least one reactor to a pressure of at least 150 mbar or less and cooling the at least one solid sorbent inside the at least one reactor to a temperature of 65° C or less; separating the product mixture into condensate and CO2in at least one separator; directing the condensate to a condensate tank; and directing the CO2to a product stream.

15. The method of capturing CO2of claim 13 or 14, wherein the steam generated by the at least one heat pump exhibits a pressure of at least 1.0 bar and a temperature of at least 100° C.

16. The method of capturing CO2of claim 13 or 14, wherein the method steps are repeated and staggered using a plurality of subsets of reactors, and wherein one subset of reactors simultaneously undergoes a different step than another subset of reactors.

17. The method of capturing CO2of claim 16, wherein a subset of reactors undergoes the step of directing ambient air through the at least one reactor containing the at least one solid sorbent while another subset of reactors undergoes the step of heating the at least one solid sorbent to a temperature between 80° and 100° C.

18. The method of capturing CO2of claim 13 or 14, wherein the heat transfer fluid is an aqueous or salt solution comprising at least 5% glycol by volume.

19. The method of capturing CO2of claim 13 or 14, wherein the at least one solid sorbent is a zeolite or amine-functionalized compound.

Images