System for separating atmospheric carbon dioxide

Abstract

A system for separating atmospheric CO2 includes a chamber containing a solid CO2 sorbent, an exchange fluid including a chemical component with selectivity towards CO2, and an electrochemical cell in fluid connection with the chamber, the system having a cycle which includes a first state of sorbent absorption of CO2 from incoming air onto the solid CO2 sorbent until a saturation point is reached, a second state of regenerating the sorbent by flooding the chamber with the exchange fluid to detach CO2 from the saturated sorbent and to bind the detached CO2 to the chemical component, and a third state of regenerating the chemical component by detaching CO2 from the chemical component in the electrochemical cell and releasing the CO2 from the system.

Description

Cross-reference to related applications

[0001] This application is a continuation-in-part of U.S. application Ser. No. 18 / 162,326, filed January 31, 2023, now pending, which is incorporated herein by reference in its entirety. field of technology

[0002] The present disclosure relates to a system for separating atmospheric carbon dioxide (CO2) using a sorbent, the regeneration of the sorbent, and a method of using the system. State of the art

[0003] Carbon dioxide is a well-known greenhouse gas whose emissions have increased rapidly since the beginning of the Industrial Revolution in the 18th century. Since then, CO2 emissions have been a proven contributor to global climate change. Recent findings from the Intergovernmental Panel on Climate Change have proposed halving CO2 emissions by 2030 to avoid further adverse impacts on the planet. Various technologies for capturing atmospheric CO2 have been developed, but their drawbacks prevent the widespread implementation of atmospheric CO2 storage. Brief description

[0004] In at least one embodiment, a system for separating atmospheric CO2 is disclosed. The system includes a chamber containing a solid CO2 sorbent, an exchange fluid including a chemical component with selectivity toward CO2, and an electrochemical cell in fluid communication with the chamber. The system has a cycle including a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent until a saturation point is reached, a second state of regenerating the sorbent by flooding the chamber with the exchange fluid to strip CO2 from the saturated sorbent and bind the stripped CO2 to the chemical component, and a third state of regenerating the chemical component by stripping CO2 from the chemical component in the electrochemical cell and releasing the CO2 from the system.The chemical component may include an amine dissolved in an aqueous solution. The first and second states may be repeated before the system proceeds to the third state. A temperature of the solid sorbent may be maintained at a constant value throughout the first, second, and third states. The third state may further include releasing the regenerated chemical component to the chamber during a second state of a subsequent cycle. The solid CO2 sorbent may be an amine-based sorbent. The CO2 bound to the chemical component formed in the second state may be released into the chamber during the first state of a subsequent cycle. The second and third states may be repeated before the system proceeds to the first state in the subsequent cycle.

[0005] In another embodiment, a system for separating atmospheric CO2 is disclosed. The system may include a chamber containing a solid amine-functionalized CO2 sorbent, a first exchange solution including a first chemical component with selectivity toward amines, a second exchange solution including a second chemical component with selectivity toward the first chemical component, and an electrochemical cell connected to the chamber.The system may comprise a first state of sorbing CO2 from incoming air onto the solid sorbent until a saturation point is reached, a second state of regenerating the solid amine-functionalized CO2 sorbent by flooding the chamber with the first exchange solution to detach CO2 from the saturated sorbent and to bind the first chemical component to the solid sorbent, removing the first exchange solution from the chamber and flooding the chamber with the second exchange solution to detach the first chemical component from the solid sorbent to bind it to the second chemical component, and a third state of regenerating the first and / or second chemical components by separating them from each other in the electrochemical cell. The CO2 may be released from the chamber in the second state.The first chemical component can include one or more metal ions. The second chemical component can include an amine. The system can be free of a heating element. The solid amine-functionalized CO2 sorbent can maintain a constant temperature during the reaction.

[0006] In yet another embodiment, a direct air capture (DAC) system is disclosed. The system may include at least one chamber containing a solid amine-functionalized CO2 sorbent, at least one exchange fluid including a first chemical component having a preferential affinity for CO2, amines, or a second chemical component, an electrochemical cell fluidically connected to the chamber, and one or more conduits configured to deliver the chemical component in a native form from the electrochemical cell to the chamber. The system may include a plurality of chambers, each fluidly connected to the electrochemical cell. The at least one exchange fluid may include a first exchange fluid and a second exchange fluid.The first exchange fluid may include a chemical component with selectivity toward CO2, and the second exchange fluid may include a chemical component with selectivity toward the first chemical component. The solid sorbent may maintain a constant temperature. The system may include a first chemical component that is different from the second chemical component.

[0007] In another embodiment, a CO2-DAC system is disclosed. The system may include a centrifuge having a cylindrical body containing a solid CO2 sorbent; an injector containing an exchange fluid path into the centrifuge; and an exchange fluid including a chemical component with a preferential affinity for CO2. The system may have a cycle including a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent and a second state of regenerating the solid CO2 sorbent by injecting the exchange fluid into the cylindrical body from the injector, rapidly rotating the cylindrical body to draw the exchange fluid through a volume of the solid CO2 sorbent, dislodging CO2 from the solid CO2 sorbent, and binding the dislodged CO2 to the chemical component.The cycle may further include a third state of regenerating the chemical component by stripping CO2 from the chemical component and releasing the CO2 from the system. The chemical component may include an amine dissolved in an aqueous solution. A temperature of the solid CO2 sorbent may be maintained at a constant value throughout the first, second, and third states of the cycle. The centrifuge may further include a central opening defined by the cylindrical body. The injector may inject the exchange fluid into the central opening. The centrifuge may further include an exchange fluid collection jacket.

[0008] In another embodiment, a CO2 DAC system is disclosed. The system may include a plurality of centrifuges, including a first centrifuge and a second centrifuge connected by a mechanical linkage. The first and second centrifuges may each contain a solid CO2 sorbent and be configured to operate in a staggered manner to remove a replacement fluid from the system after the replacement fluid has bound CO2. The first and second centrifuges may include the same solid CO2 sorbent. Each of the first and second centrifuges may include a cylindrical body containing the solid CO2 sorbent. The mechanical linkage may be a flywheel.The staging may include operating the first centrifuge for one cycle and then mechanically transferring mechanical energy from the first centrifuge to the second centrifuge. The cycle may include a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent. The cycle may include a second state of regenerating the solid CO2 sorbent by injecting the exchange fluid containing a chemical component with a preferential affinity for CO2 into the first centrifuge, rapidly rotating the centrifuge to draw the exchange fluid through a volume of the solid CO2 sorbent, dislodging CO2 and binding the dislodged CO2 to the chemical component. The solid CO2 sorbent may include an amine dissolved in an aqueous solution.A temperature of the solid sorbent can be maintained at a constant value throughout the first and second states of the cycle.

[0009] In another embodiment, a CO2-DAC system is disclosed. The system may include a first group of centrifuges, each having a body containing a solid CO2 sorbent; a second group of centrifuges, each having a body containing a solid CO2 sorbent; a mechanical linkage connecting the first group to the second group; an injector configured to provide an exchange fluid in each centrifuge; and the exchange fluid including a chemical component with a preferential affinity for CO2. The system may include a cycle of CO2 sorption onto the solid CO2 sorbent and CO2 desorption from the exchange fluid in the first group of centrifuges, followed by the cycle in the second group of centrifuges. The cycle may include a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent.The cycle may include a second stage of regenerating the sorbent by injecting the exchange fluid into the first group, rapidly rotating the first group to draw the exchange fluid through a volume of sorbent in each centrifuge, dislodging CO2 from the solid CO2 sorbent and binding the dislodged CO2 to the chemical component. Mechanical energy from the first group of centrifuges may be transferred mechanically to the second group of centrifuges via the mechanical linkage. The mechanical linkage may be a flywheel. The centrifuges in the first group of centrifuges may have a cylindrical body. BRIEF DESCRIPTION OF THE DRAWINGS Fig. Figure 1 is a schematic representation of a prior art direct air capture (DAC) process in which regeneration of CO2 sorbent requires a change in temperature, pressure, humidity, or other stimulus; Fig. Figure 2 shows a schematic representation of an EMAR (electrochemically mediated amine regeneration) process using a liquid sorbent to separate CO2 from concentrated sources; Fig. 3 is a schematic representation of a non-limiting exemplary system in accordance with one or more embodiments disclosed herein, providing multiple chambers of solid CO2 sorbent connected to a common electrochemical cell; the Fig. 4A and Fig. 4B shows a schematic representation of non-limiting exemplary systems in accordance with one or more embodiments disclosed herein, in which a single exchange fluid is used to regenerate a solid CO2 sorbent; Fig. 5 is a schematic representation of another non-limiting exemplary system in accordance with one or more embodiments disclosed herein, using multiple exchange fluids to regenerate a solid CO2 sorbent; Fig. 6 is a schematic representation of a non-limiting exemplary centrifuge disclosed herein; and Fig. Figure 7 is a schematic representation of a plurality of non-limiting exemplary connected centrifuges for continuous operation of the systems described herein. DETAILED DESCRIPTION

[0010] Embodiments of the present disclosure are described herein. However, it is understood that the disclosed embodiments are only examples, and other embodiments may take various and alternative forms. The figures are not necessarily to scale; some features may be exaggerated or minimized to show details of particular components. Therefore, specific structural and functional details disclosed herein are not to be interpreted as limiting, but merely as a representative basis for teaching one skilled in the art the various uses of the present embodiments.As will be understood by those of ordinary skill in the art, various features illustrated and described with reference to any of the figures may be combined with features illustrated in one or more other figures to develop embodiments not explicitly illustrated or described. The combinations of illustrated features provide representative embodiments for typical applications. However, various combinations and modifications of the features consistent with the teachings of this disclosure may be desirable for particular applications or implementations.

[0011] Except for the examples, or unless otherwise expressly stated, in describing the broadest scope of the disclosure, all numerical quantities in this specification indicating amounts of material or reaction and / or use conditions are to be understood as modified by the word "about." Practice within the listed numerical limits is generally preferred.In addition, unless expressly stated to the contrary: percent, "parts of," and ratios are by weight; the description of a group or class of materials as suitable or preferred for a given purpose is accompanied by a disclosure that mixtures of any two or more of the elements of the group or class are equally suitable or preferred; a description of ingredients in chemical terms refers to the ingredients at the time of addition to any combination specified in the description, and does not necessarily preclude chemical interactions between the ingredients of a mixture after they have been mixed.

[0012] The initial definition of an acronym or other abbreviation applies to all subsequent uses of the same abbreviation herein and applies mutatis mutandis to normal grammatical variations of the originally defined abbreviation. Unless otherwise noted, the measurement of a property is determined by the same technique previously or subsequently referenced for the same property.

[0013] It should also be noted that the singular forms "a," "an," "another," and "the" used in this specification and the appended claims also include plural references unless the content clearly indicates otherwise. For example, a reference to a component in the singular is intended to include a plurality of components.

[0014] The term "substantially," "generally," or "about" as used herein means that the amount or value in question may be the specific value designated or some other value nearby. Generally, the term "about," when used to designate a particular value, is intended to designate a value within ± 5% of the value. As an example, the term "about 100" designates a range of 100 ± 5, i.e., the range from 95 to 105. When the term "about" is used, it is generally expected that similar results or effects according to the disclosure can be obtained within a range of ± 5% of the recited value. The term "substantially" may modify a value or relative characteristic disclosed or claimed in the present disclosure. In such cases, "substantially" may mean that the value or relative characteristic disclosed or claimed iswhich is modified thereby is within ± 0%, 0.1%, 0.5%, 1%, 2%, 3%, 4%, 5% or 10% of the value or relative characteristic.

[0015] It should also be recognized that an integer range explicitly includes all intermediate integers. For example, the integer range 1-10 explicitly includes 1, 2, 3, 4, 5, 6, 7, 8, 9, and 10. Similarly, the range 1 to 100 includes 1, 2, 3, 4... 97, 98, 99, 100. Similarly, if an arbitrary range is required, intermediate numbers that are increments of the difference between the upper and lower bounds divided by 10 may be used as alternative upper or lower bounds. For example, if the range is 1.1 to 2.1, the following numbers, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, and 2.0, may be chosen as lower or upper bounds.

[0016] In the examples given here, concentrations, temperature, and reaction conditions (e.g., pressure, pH, flow rates, etc.) can be practiced to plus or minus 50 percent of the specified values, rounded or truncated to two significant figures of the value given in the examples. With further refinement, concentrations, temperature, and reaction conditions (e.g., pressure, pH, flow rates, etc.) can be practiced to plus or minus 30 percent of the specified values, rounded or truncated to two significant figures of the value given in the examples. With further refinement, concentrations, temperature, and reaction conditions (e.g., pressure, pH, flow rates, etc.) can be practiced to plus or minus 10 percent of the specified values, rounded or truncated to two significant figures of the value given in the examples.

[0017] For all compounds expressed as an empirical chemical formula with multiple letters and numerical subscripts (e.g., CH2O), values ​​of the subscripts may be plus or minus 50 percent of the values ​​rounded or truncated to two significant figures. For example, if CH2O is given, a compound of formula C (0,8-1,2) H (1,6-2,4) O (0,8-1,2) . With one refinement, values ​​of subscripts may represent plus or minus 30 percent of the listed values, rounded or truncated to two significant figures. With yet another refinement, values ​​of subscripts may represent plus or minus 20 percent of the listed values, rounded or truncated to two significant figures.

[0018] The term "and / or" used here means that either all or only one of the elements of the group can be present. For example, "A and / or B" means "only A or only B or both A and B." In the case of "only A," the term also covers the possibility that B is absent, i.e., "only A but not B."

[0019] It is also understood that this disclosure is not limited to the specific embodiments and methods listed below, as specific components and / or conditions may naturally vary. Furthermore, the terminology used herein is used only for the purpose of describing particular embodiments of the present disclosure and is not intended to be limiting in any way.

[0020] The term "comprising" is synonymous with "including," "having," "containing," or "characterized by." These terms are inclusive and not limiting and do not exclude additional, unstated elements or process steps.

[0021] The term "consisting of" excludes any element, step, or component not listed in the claim. When this term appears in a definition of the subject matter of a claim rather than immediately following the preamble, it limits only the element listed in that term; other elements are not excluded from the claim as a whole.

[0022] The term “consisting essentially of” limits the scope of a claim to the specified materials or steps and those which do not substantially affect the basic and novel feature(s) of the claimed subject matter.

[0023] With respect to the terms "comprising," "consisting of," and "consisting essentially of," the subject matter disclosed and claimed herein may include the use of either of the other two terms when either of those three terms is used herein.

[0024] The term "one or more" means "at least one," and the term "at least one" means "one or more." The terms "one or more" and "at least one" include a "plurality" as a subset.

[0025] The description of a group or class of materials as suitable for a given purpose in connection with one or more embodiments implies that mixtures of two or more members of the group or class are suitable. A description of components as chemical terms refers to the components at the time of addition to any combination specified in the description and does not necessarily preclude chemical interactions between components of the mixture after mixing. An initial definition of an acronym or other abbreviation applies to all subsequent uses of the same abbreviation herein, and it applies mutatis mutandis to normal grammatical variations of the initially defined abbreviation. Unless otherwise noted, the measurement of a property is determined by the same technique previously or subsequently referenced for the same property.

[0026] Carbon dioxide, or CO2, is a major greenhouse gas, accounting for about 80% of all greenhouse gas emissions from human activities in the United States each year. CO2 emissions are a recognized global problem. Greenhouse gases are gases that trap heat in the atmosphere. This heat trapping causes changes in Earth's radiation budget, which alters climate and weather patterns on a global and regional scale. CO2 is a chemical compound composed of molecules, each with one carbon atom bonded to two oxygen atoms by covalent double bonds. CO2 exists in a gaseous state at ambient temperature. In the air, CO2 is transparent to visible light but absorbs infrared radiation, acting as a greenhouse gas. CO2 enters the atmosphere through the burning of fossil fuels such as coal, natural gas, and oil, solid waste, trees, and other biological materials.CO2 also enters the atmosphere as a result of certain chemical reactions, such as the production of cement or aluminum. Furthermore, when methane enters the atmosphere, it combines with oxygen to form CO2.

[0027] Due to its negative impact on the global climate, efforts to reduce CO2 emissions have been primarily undertaken by capturing CO2 at the source of release, such as from the chimneys of power plants, cement plants, or aluminum plants. However, many man-made CO2 emissions, such as those from motor vehicles or aircraft, cannot be captured at the source. Furthermore, capturing CO2 already released, known as legacy CO2, is highly desirable to reduce the overall climate impact of the greenhouse gas CO2.

[0028] Therefore, the extraction of CO2 from ambient air is a potential route to reducing greenhouse gas emissions and the associated climate change. Direct extraction of CO2 from air using a sorbent, typically referred to as Direct Air Capture (DAC), represents the gold standard technology for this goal. A typical DAC sorption process includes two steps, which are Fig. 1 are shown schematically.

[0029] As from Fig. 1, in the first stage or step 1, a sorbent 20 selected to selectively absorb CO2 is exposed to air until it reaches a desired saturation point. In the first step of Fig. 1, air is passed over an amine-functionalized sorbent 20, which separates CO2 from the incoming gas stream, referred to as air. In the second stage, or step 2, the sorbent is regenerated by stripping the absorbed CO2 from the sorbent 20 and storing the separated CO2 at high pressure and with high purity for later use or storage, which is labeled B. In the second step, the CO2 bound to the solid sorbent 20 is separated using a change in temperature, pressure, humidity level, or other stimulus, labeled A, which regenerates the sorbent to its original state and releases the CO2 for storage or use. The process can then be repeated. In the diagram, the line connecting "amine" to "porous support" indicates that the amines are chemically bonded to the support.

[0030] While the first step of this process is spontaneous because the sorbent chemistry is chosen to promote a favorable reaction with CO2, the regeneration step requires an energy input to desorb the captured CO2. This energy can be supplied in the form of heat, changes in external pressure, changes in humidity, or potential. The energy cost of the DAC process, as well as the useful life of the sorbent material, is largely determined by the effectiveness of the regeneration step, making it an important design component of any DAC process. In general, high energy requirements for sorbent desorption represent a barrier to successful use of the process. Furthermore, the heat typically used for desorption is such that sorbent damage often occurs due to thermal and oxidative stress.Furthermore, the desorption efficiency is limited, so that typically less than 100% of the sorbent is isolated, with the recovery efficiency decreasing over time.

[0031] In DAC, a typical sorbent technology includes a porous support material functionalized with amine-containing molecules or polymers. For example, a porous silica or cellulose support material can be functionalized with amine-containing molecules or polyethyleneimine (PEI). In this type of sorbent, the amines react spontaneously with CO2, thereby separating the CO2 from the air. The porous support material provides a high specific surface area for the amine / air interface, ensuring that air can flow through the sorbent and anchoring the amines in the solid sorbent, preventing their volatilization.

[0032] State-of-the-art supported amine-based solid sorbent systems are typically regenerated by heating to a temperature of approximately or above 100 °C, at which CO2 no longer binds favorably to the amines, by exposure to high-temperature steam, by exposure to negative pressure, or by a combination of the above. These regeneration processes are highly energy-intensive, and in the case of high-temperature desorption, they contribute to the degradation of the amine sorbent through thermal degradation and oxidation. Therefore, such systems are unsustainable.

[0033] A relatively new technology emerged in the field of CO2 sequestration from concentrated sources such as power plant emissions. Such sequestration scenarios do not involve capture from the atmosphere, but instead CO2 capture directly at the source. Such capture occurs from concentrated CO2 streams, not from diluted sources such as air. Thus, these systems differ in terms of components and configuration.

[0034] For example, systems for separating a CO2 stream can use liquid sorbents. The CO2-containing gas is bubbled through a liquid containing amine-containing molecules that react favorably with CO2. The liquid sorbent solution can then be regenerated by heating, similar to the solid sorbent. However, a more effective approach is to remove the absorbed CO2 electrochemically using a process known as electrochemically mediated amine regeneration (EMAR). As described in Fig. As shown in Figure 2, the EMAR process involves pumping the CO2-saturated amines through a series of tanks in which Cu metal is electrochemically removed, producing Cu 2+ -ions are formed, which then displace the absorbed CO2, releasing the displaced CO2 as a high-pressure gas for storage, and Cu bound to the amines 2+Ions are electrochemically deposited as Cu metal, regenerating the amine sorbent to its initial state. The EMAR process has been proven to be energetically competitive with thermal regeneration, offering advantages in terms of modularity and thermal management.

[0035] Fig. Figure 2 shows a schematic representation of the electrochemical cell system 100 designed to carry out the EMAR process. Fig. Figure 2 shows a liquid sorbent 120', in particular a liquid amine-containing solution (R-NH2), which is saturated with CO2 in the sorbent tank 105. The liquid sorbent solution 120' is heated by an electrochemical cell 130 with a Cu 2+ -ions containing first chamber 132, a second chamber 134 and a membrane 136 which separates the chambers 132, 134. The solution 120' is first pumped into a first chamber 132 of the Cu 2+-ions, where the Cu ions are exchanged with the CO2 bound to the amines, which is marked as step (a). The Cu-exchanged and CO2-containing solution is then pumped to a flash tank 110, which is marked as step (b), where CO2 is outgassed to a storage facility B, which is marked as step (c). Finally, the Cu-bound amines are regenerated in the second chamber 134 of the electrochemical cell 130 by electrochemically depositing Cu on a Cu electrode 138 and pumping the original amines back to the sorbent tank 105. For the electrochemical cell 130 to function, the cell contains a supporting electrolyte with a Cu salt 140 and the anion exchange membrane 136, which allows the supporting anions from the electrolyte salt to pass through but blocks the Cu cations.

[0036] Liquid sorbent systems are typically pumped systems that use multiple tanks or chambers to move liquid between locations. CO2 is typically pumped from the initial sorbent tank to one or more containers before it can be removed from the system. This increases space requirements, complexity, and cost.

[0037] The use of liquid amine sorbents has not been feasible in DAC applications because the high air volumes required to be processed volatilize the sorbent, resulting in unacceptable losses. Furthermore, the requirement that a DAC sorbent be a solid has precluded the use of electrochemical regeneration schemes such as the EMAR in previously published DAC applications.

[0038] Nevertheless, there is an urgent need to improve atmospheric CO2 sequestration systems, especially for the regeneration of amine-based sorbents, so that humanity can reduce the concentration of CO2 emissions and remove the CO2 legacy from the air to prevent further progression of climate change.

[0039] In one or more embodiments, a system is disclosed that is designed to sequester CO2 from dilute sources. The system may be a DAC system. The system is arranged to separate CO2 from air, the atmosphere. The separation may be direct separation. The CO2 may be anthropogenic CO2, a CO2 legacy, naturally produced CO2, CO2 from various sources such as decomposition CO2, CO2 released from the ocean, respiratory CO2, CO2 from industrial sources, CO2 from deforestation, CO2 from the combustion of fossil fuels, CO2 from transportation, CO2 from the combustion of fuels, exhaust CO2, and the like, or a combination thereof. The system includes multiple components that interact mechanically, physically, chemically, fluidly, or through a combination thereof. Non-limiting examples of the systems disclosed herein are described in the Fig. 3, Fig. 4A, Fig. 4B and Fig. 5 shown.

[0040] The system disclosed herein includes at least one container. The system may include 2, 3, 4, 5, 6, or more containers. However, the system may also include a single container or only two containers. The container may be a tank, a container, a chamber, a canister, a capsule, a tub, a chamber, a basin, a flask, a vessel, or the like. The container may be a closed, closable, openable, sealable, and / or resealable container.

[0041] The container may enclose or contain a solid CO2 sorbent with a porous support and amine-based chemistry attached to or immobilized on the support. The sorbent may be a solid amine sorbent. The sorbent may be a DAC sorbent. The sorbent may be an amine-functionalized sorbent. Amine-based sorbents enable efficient absorption of CO2 due to high chemical reactivity toward CO2 and relatively low cost. Non-limiting exemplary support materials may include mesoporous silica or polymeric materials such as cellulose, polymethyl methacrylate (PMMA), or polystyrene (PS). The amine may be incorporated by impregnation, grafting, or the like.

[0042] The container may include one or more air inlets configured as resealable or closable openings, and one or more conduits connecting one or more sections of the system and arranged to convey one or more fluids between different sections of the system. The fluids may be air, exchange fluid(s), electrolyte(s), etc.

[0043] The system may further include one or more exchange fluids or solutions. The system may include a first exchange fluid and a second exchange fluid, which may be the same or different. The exchange fluids may differ in terms of their volume, composition, and / or other properties. An exchange fluid may be a fluid or solution including a chemical component that strips a previously bound component from the solid sorbent. The previously bound component may be CO2, electrochemical intermediates associated with CO2, metal ion(s), M1, or a combination thereof. The component may exhibit selectivity, preferably affinity, and / or high chemical reactivity toward the CO2, another chemical component, or amines.A selectivity or preferential affinity of the component can be defined as the difference shown by a reagent (a component) in a competitive attack against two or more substances (such as CO2 and amines or M1 and amines).

[0044] In one non-limiting example, the exchange fluid may include a component designed to bind to CO2 so tightly that when the exchange fluid comes into contact with the CO2 bound in the solid sorbent, the CO2 is removed from the sorbent and instead bound to the component. In another non-limiting example, the exchange fluid may include a component designed to bind to amines so tightly that when the exchange fluid comes into contact with the CO2 bound in the solid sorbent, the CO2 is removed from the sorbent and instead bound to the component.In yet another non-limiting example, an exchange fluid may include a component designed to bind to another component, such as a metal ion(s), so strongly that when the exchange fluid comes into contact with the other component (metal ion(s)) previously bound in the solid sorbent, the other component (metal ion(s)) is removed from the sorbent and instead binds to the component.

[0045] The exchange fluid may be provided, configured, or adapted to remove CO2 from the solid sorbent, the system, or both, and / or to regenerate the solid sorbent. The exchange fluid is thus configured to mediate transport of CO2, related electrochemical intermediates, and / or other components in the systems disclosed herein. For example, the one or more exchange fluids may be configured to mediate transport of CO2, related electrochemical intermediates, and / or other components between the solid sorbent in the at least one chamber and the electrodes of the electrochemical cell. The exchange fluid enables the use of a single chamber that can be flooded and drained with one or more exchange fluids during steps one, two, and / or three.

[0046] The exchange fluid may be an aqueous solution. A non-limiting example of the exchange fluid may be a pure amine liquid or a liquid mixture of amines. The component in the exchange fluid may include one or more molecules of M1 or M2. The M1 molecules may be metal ion(s). A non-limiting example of the metal ions may be Cu 2+ , Zn 2+ , Pb 2+ , Ag 2+ , Mg 2+ or Al 3+M1 may be present or dissolved in the exchange fluid. The exchange fluid may be provided in the at least one chamber after a desired and / or predetermined level of CO2 saturation in the solid sorbent is reached. M1 may be chemically designed to bind to the solid sorbent amines and thus remove, desorb, or replace CO2 previously absorbed on the solid sorbent. In other words, the CO2 may be removed or stripped from the solid sorbent, and instead, M1 may bind to the sorbent. A non-limiting example of such a chemical component M1 is described in Fig. 5 and Example 2.

[0047] The molecule(s) M2 may be dissolved in the exchange fluid. The exchange fluid may be provided in the at least one chamber after a desired and / or predetermined level of CO2 saturation in the solid sorbent is reached. The molecules M2 may be chemically designed to bind the CO2 previously absorbed on the solid sorbent. In other words, the CO2 may be removed or stripped from the solid sorbent into a dissolved state and instead bind to the molecule M2. A non-limiting example of such a chemical component M2 is described in the Fig. 4A, Fig. 4B and Example 1.

[0048] M2 can be ethylenediamine (EDA), diethylenetriamine (DETA), triethylenetetramine (TETA), monoethanolamine (MEA), or another small molecular amine. The solute molecule M2 in the exchange solution can be chosen based on the binding energy between M2, CO2, and / or the metal ion(s) M1. M2 can be chosen such that the binding energy between M1 and M2 is greater than that between M1 and the solid amine sorbent. M2 can be chosen such that the binding energy between M2 and CO2 is greater than that between CO2 and the solid amine sorbent.

[0049] The system further includes an electrochemical cell. The electrochemical cell may include one or more chambers, such as the first chamber and the second chamber. The chambers may be separated by a membrane that is semipermeable, selectively permeable, or nonpermeable to one or more chemical species, components, or ions. The cell may include an electrolyte. The electrolyte may include a salt solution. A non-limiting example solution may be a Cu salt solution. Other salt solutions may include Zn, Pb, Ag, Mg, Al, or other metals. Each chamber may include an electrolyte, a cathode, or an anode, respectively. The electrodes may be symmetrical or asymmetrical. The electrodes may include metal ions such as M1. The electrodes may include a metallic form of the M1 elements, such as Cu, Zn, Pb, Ag, Mg, Al, or the like. The electrode(s) may include one or more layered oxides of form (M1).a (X)O z where X is V, Cr, Mn, Ni, Co or Fe; with 0 < a < 1 and 1.9 < z < 2.6.

[0050] The cell may further include an electrical circuit connecting the electrodes and including a voltage source. The cell may be connected to the at least one container via one or more leads. The electrochemical cell may be provided, designed, or configured to regenerate the molecule M1, M2, or both, and / or release CO2.

[0051] The system disclosed herein may have one or more states, stages, or steps. For example, the system may have 1, 2, or 3 states. Each state may be repeatable. Each state may include one or more cycles. In the first state, the CO2 sorbent may bind CO2 up to a predetermined point. The predetermined point may reflect a full or partial saturation point or a predetermined degree of CO2 saturation. In the first state, the air may exit the system, the chamber, or both with a lower CO2 concentration. The first state may be a state of CO2 saturation and / or CO2 release.

[0052] In the second state, the chamber can be flooded with one exchange fluid. The chamber can be flooded with two exchange fluids separately. The exchange fluids can be individually supplied and discharged in the vessel. In the second state, the CO2 can be removed from the solid sorbent and released from the chamber. In the second state, the solid sorbent can be regenerated via the exchange fluid(s), which include a component M1, M2, or both. The second state can be a state of CO2 desaturation and release and / or a regeneration of the solid sorbent.

[0053] In the third state, the exchange fluid containing M1, M2, an M1-M2 complex(es), and / or M2-CO2 can be removed from the solid sorbent-containing chamber and provided to an electrochemical cell. In the electrochemical cell, a component chemistry and / or a voltage can be used to regenerate M1, M2, or both. In the electrochemical cell, CO2 can be removed from M2-CO2 and released for storage and / or use. The third state can be a regeneration state of M1, M2.

[0054] The system may lack, or be free of, a heating element (internal or external), for example, a heating element connected to the one or more chambers containing the solid sorbent or influencing and increasing the temperature. The temperature of the system and the sorbent in stages one, two, and / or three may be relatively constant, without fluctuations, without desirable or predetermined fluctuations, without an increase above 70°C, 80°C, 90°C, 100°C, 110°C, 120°C, 130°C, or more. The temperature of the sorbent may be maintained, held, or maintained at a relatively constant value throughout the first, second, and third states.

[0055] The system may include a single chamber containing the solid CO2 sorbent so that CO2 removal can occur within the single chamber. The single chamber may enclose the solid sorbent capturing the CO2, and the CO2 may be released from the single chamber after the chamber has been flooded with an exchange fluid. After flooding, the CO2 may be released directly into storage and / or for use. Alternatively, after flooding, the CO2 may be bound to an M2 molecule and remain in the chamber, from which the exchange fluid can be vented, an air inlet opened, and a next cycle or round of CO2 sorption onto the solid sorbent can occur.

[0056] In conventional liquid sorbent systems, the entire volume of liquid sorbent with the bound CO2 is typically pumped through the electrochemical cell's regeneration system. The final CO2 efficiency is thus determined by the entire process, including sorption and regeneration. In contrast, the system disclosed here has physically separate sorption and desorption stages and the regeneration of stages M1, M2. Thus, with the system disclosed here, the efficiency of CO2 removal can be increased by having multiple cycles of CO2 sorption (first stage), solid sorbent regeneration (second stage), or both prior to the regeneration of M1, M2, or both initiated due to the possibility of repeated flooding and venting with the exchange fluid(s).Similarly, the process disclosed herein may include multi-stage regeneration of M1, M2 to increase the efficiency of regeneration of M1, M2, or both. In one or more embodiments, the second and third steps may be repeated before the first step begins in the next cycle.

[0057] In one or more embodiments, a mechanism for regenerating the solid sorbent may include a mechanical device, mechanical forces, and a transfer of mechanical energy. The mechanism may be part of the solid sorbent regeneration or the second stage. The mechanism may force the exchange fluid through the porous sorbent to separate CO2. The mechanism may be active or activated after the solid sorbent is exposed to air and saturated with CO2. An exchange fluid absorbing the CO2 must be moved through the solid sorbent, binding the CO2 and removing the CO2 from the solid sorbent with the exchange fluid.

[0058] The mechanism may include gravitational forces to force CO2 and the exchange fluid through the sorbent. Alternatively, or in addition, other forces may be used. These other forces may include centrifugal forces.

[0059] Centrifugation represents a mechanical approach for separating fluids from solids with much lower energy costs than heat- or vacuum-based drying. Although centrifugation cannot remove all fluid from a porous solid, it can be used to remove a large fraction of the fluid from macropores and interstitial volume, significantly reducing the burden on subsequent drying steps. Centrifugation can be used to remove the exchange or transfer fluid containing M1, M2, or the M1-M2 complex(es) from the system after they have bound CO2.

[0060] The solid sorbent DAC system described herein can be configured to allow centrifugation of the solid sorbent as one of the steps in the fluid-based regeneration process. As a non-limiting example, the solid sorbent can be shaped into a cylinder or have a cylindrical body. Other shapes are contemplated. The cylinder can be a hollow cylinder or a cylinder with a hollow center or opening, and the body forms the hollow center or opening. The body encloses the sorbent material. The thickness of the body defines the volume of the cylinder or sorbent. The body can have an inner surface and an outer surface.

[0061] The centrifuge may further include a rotor assembly (not shown) and an electric motor (not shown). The rotor assembly transmits the rotational force generated by the electric motor. The rotor assembly may include a drive shaft and a rotor. The motor converts electrical energy into mechanical energy and provides the rotational motion.

[0062] The injection of the exchange fluid can be accomplished by means of an injector. The injector can be any device or apparatus designed to effectively introduce the fluid into the centrifuge. The injector can introduce the fluid by spraying, trickling, splashing, squirting, etc. The injector can include a nozzle, a valve, or both. The injection can be continuous, discontinuous, at the same or a different pressure, volume, at a different altitude, temperature, etc. The injector can include a route for the exchange fluid into the centrifuge. The injector can inject the exchange fluid into the central opening, the centrifuge body, or both.

[0063] The exchange fluid can be injected into the center of the cylinder, onto or into the body, or a combination thereof. The cylinder can be rapidly rotated at a high speed to draw the fluid through the cylinder body, absorbing any CO2 bound to the solid. During the process, the fluid is drawn through the inner surface, the body, to the outer surface. The fluid with the bound CO2 can thus be expelled from the sorbent. The fluid with the CO2 can then be collected at an outer radius or surface of the cylinder. A non-limiting example of the regeneration cycle is described in Fig. 6 is shown schematically.

[0064] Fig. Figure 6 shows a fluid-based regeneration system configured for removing exchange fluid by centrifugation. A single sorbent cylinder 400 includes a CO2 transfer fluid injection / injector 401 in the center of the cylinder 400 or within the central opening 403 of the cylinder 400. Additional or alternative injection into the cylindrical body is also provided. The cylinder 400 further includes the body 402 and a fluid collection container 404 on the outer surface 405. The fluid exchange collection container 404 can be a casing, a container, a pipe, a conduit, a tank, or other suitable structure. The exchange fluid can be drawn through the volume of sorbent by centrifugation or rotation of the cylinder. Movement of the exchange fluid alone and later of the fluid with absorbed CO2 is shown. The rotation of the centrifuge is shown in Fig. 6 illustrated by an arrow.

[0065] The system can have various states. The first state can be the state of sorbing CO2 from incoming air onto the solid CO2 sorbent. The second state can be the state of regenerating the solid CO2 sorbent by injecting the exchange fluid from an injector into the centrifuge, rapidly rotating the centrifuge to draw the exchange fluid through a volume of the solid CO2 sorbent, whereby CO2 is released from the solid CO2 sorbent and the released CO2 binds to the chemical component. The third state can be the state of regenerating the chemical component by releasing CO2 from the chemical component and releasing the CO2 from the system.

[0066] The solid sorbent and the exchange fluid may be part of a system including a plurality of centrifuges. The plurality may include 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more centrifuges. The plurality may include a first centrifuge and a second centrifuge. Each centrifuge may include a solid CO2 sorbent.

[0067] The centrifuges can be staggered. The solid sorbent can thus be arranged in a system of centrifuges, such as those with cylinders that operate in staggered fashion. The cylinders rotate one after the other. The staggering can involve operating a first centrifuge for one cycle and then mechanically transferring mechanical energy from the first centrifuge to the second centrifuge.

[0068] Staggering is desirable to implement a continuous flow of exchange or transfer fluid(s) with absorbed CO2 from the system to enable continuous operation of downstream operating units. This is in contrast to operating all cylinders at once, which would not result in a continuous process. Because energy input is required and energy is lost each time a system needs to be started or stopped, a continuous process is the most desirable method for operating an efficient system. Operational staggering of cylinders thus enables energy transfer instead of repeatedly stopping and starting the system.

[0069] A subset of cylinders, including one or more cylinders, can be centrifuged at a time, as described above. At the end of the centrifugation cycle, the mechanical energy of the rapidly rotating cylinders can be mechanically transferred to the next set of cylinders. The mechanical transfer can be achieved via a direct mechanical coupling, a flywheel, or other means. In this system, the centrifugation system can operate with minimal energy dissipation, enabling maximum energy efficiency and the continuous flow of saturated regeneration fluid.

[0070] The number of cylinders can vary and can be 1, 2, 3, 4, 5, 6, 7, 8, 9, or more in each subgroup. The cylinders can be identical or different from one another. For example, at least one of the cylinders can have a capacity, volume, dimensions, or other property that is different (larger or smaller) than that of at least one other cylinder. The cylinders can be spaced apart in a regular or irregular manner or pattern. The sorbent in the cylinders can be the same or different, having one or more identical or different properties, such as chemical composition, density, volume, etc.

[0071] A non-limiting example of a multi-centrifuge system is shown in Fig. 7, schematically depicting a system 420 of a number of sorbent cylinders 400 for efficient and continuous operation, wherein the cylinders 400 are formed in groups of one, two, or more at a time, with a mechanical linkage interconnecting the cylinders 408 to transfer mechanical energy between the cylinders 400 at the end of a centrifugation cycle. Because the systems described herein may utilize a single chamber containing the solid CO2 sorbent, the effectiveness of CO2 removal may be determined by the amount of fluid introduced and removed, the amount of fluid recirculated, etc. In one or more embodiments, about 80-100, 82-98, or 85-95 vol.-% of the first exchange fluid, the second exchange fluid, or both added during a given cycle are removed from the system at a predetermined time or interval.

[0072] In the systems described here, the EMAR or electrochemical cell can be used only to regenerate the M1, M2, or both molecules, while the sorbent regeneration and / or CO2 release can occur in the original chamber. This is in contrast to liquid sorbent systems, where the entire volume of CO2-bound liquid sorbent is typically pumped through the EMAR system. The EMAR or electrochemical cell is thus required as a middle step for CO2 removal in the conventional system, but not in the system disclosed here.

[0073] In one or more embodiments, the system described herein may include multiple chambers, each containing a solid sorbent. A non-limiting example of such a system 500 is shown in Fig. 3. The multiple chambers 502 may be flooded and drained one or more times before initiating the regeneration stage for M1, M2, M1-M2, and / or M2-CO2 in the electrochemical cell 530. In other words, the system may include 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more chambers 502, each having states one and two, or switchable between them. 502 may correspond to 202, 302, or another configuration of the chamber. The system may also include a single regeneration system configured as an electrochemical cell or EMAR 530, providing the third state. 530 may correspond to 230, 330, or another configuration of the cell. The single regeneration system 530 may be common to all containers 502.The system may thus include an electrochemical cell fluidically connected to the multiple chambers and receiving the one or more exchange fluids from the multiple chambers. Such a system has the advantage of lower capital expenditure.

[0074] For the multiple chambers, the chemistry of the exchange fluids and their components can be the same or different. The volumes of the chambers and the exchange fluids can be the same or different. The individual cell can receive the fluids from at least some or all of the chambers simultaneously. Alternatively, the individual cell can receive the fluids from different chambers in a predetermined manner, randomly, scheduled, sequentially, two at a time, etc.

[0075] Thus, the system disclosed here can be combined with a solid DAC sorbent for electrochemical regeneration for direct capture of atmospheric CO2 or capture of CO2 from dilute sources such as air. The advantages of the system described here include an energy-efficient route for regenerating solid amine sorbents without the need for heating, which offers significant advantages in terms of improved energy efficiency, increased sorbent lifetime, simplified thermal management, and modularity. Particularly with regard to thermal management, high heat or steam are not required for sorbent regeneration. The sorbents themselves are not subject to thermal degradation, and the system's energy requirements are lower than those of prior art systems. EXAMPLESExample 1

[0076] In at least one embodiment described in the Fig. 4A, Fig. 4B, a non-limiting exemplary system 200 may include a chamber 202 having an opening 204 configured as an air inlet. The chamber 202 may include a solid amine-functionalized sorbent 220. The system may have one or more states, steps, or stages. In the first state, the CO2 from the air entering the chamber 202 is bound to the amine of the sorbent 220, and air with a lower CO2 concentration exits via an opening 206 configured as an air outlet. In the first state, the air in the chamber 202 may be passed through the solid amine-functionalized sorbent 220 until a desired or predetermined CO2 concentration is reached.

[0077] In the second state, second stage, or second step, the external air flow is stopped, and the sorbent 220 is regenerated. For the purposes of regeneration, the sorbent 220 in the chamber 202 can be flooded with a solution 240 containing dissolved M2 molecules. The CO2 can be stripped from the solid sorbent 220 with the solution 240. The M2 molecule can bind to the CO2 more strongly than the solid amine, so the CO2 transitions from binding to the solid sorbent 220 to binding to the M2 molecule. Once the aqueous M2-CO2 solution has removed a desired amount of CO2 from the solid sorbent, the solution can be separated from the solid sorbent, allowing the sorbent to return to the first state, ready for additional CO2 removal in the next cycle. The separation can be accomplished by discharging the M2-CO2 solution through the outlet port 206 or another port.The solid sorbent 220 is thus regenerated via the exchange solution 240, not an EMAR or an electrochemical cell.

[0078] The centrifuge described above can be used in the stage for regenerating the solid sorbent of the Fig. 4A. The centrifuge or a staggered system of a plurality of centrifuges may be included in the second stage. The M2 molecule, which forms part of the exchange fluid, would be injected into the cylindrical sorbent enclosing absorbed CO2. Centrifugal forces would push the M2 molecule, which would absorb the CO2, through the cylinder volume to the outer surface of the cylinder. At the time of M2-CO2 expulsion from the centrifuge, the M2-CO2 would pass to the third stage.

[0079] In system 200, an electrochemical cell 230 can be used to regenerate the M2 molecule to the third state. The vented M2-CO2 solution can either be reused for the second state in the subsequent cycle(s), passed through an EMAR cycle to regenerate the M2 molecule and extract the bound CO2, or both.

[0080] In a third state, stage, or step, an electrochemical cell 230 is used when the M2-CO2 solution is passed through the EMAR cycle. A non-limiting example of the EMAR system with the M2-CO2 solution is shown in Fig. 4B is shown schematically.

[0081] The electrochemical cell 230 may include a membrane 242 separating two chambers 244, 246, each containing an electrode 248 (cathode) and 250 (anode). The electrodes may be connected to a voltage source 254 via an electrical circuit 252. The electrochemical cell 230 may be flooded with an electrolyte 256, such as a Cu salt electrolyte.

[0082] The M2-CO2 solution enters the first chamber 244 of the cell 230, the Cu 2+ -ions. The Cu 2+Ions are exchanged with the CO2 bound to the M molecule. The M2-Cu solution together with CO2 can be moved to a tank 260. The movement can be accomplished by pumping, draining, or otherwise. CO2 can be removed directly from the first chamber 244. CO2 can be driven off to a storage facility or removed from the system 200. The M2-Cu solution can be moved via the tank 260 or directly into the second chamber 246 of the cell 230, for example, by pumping or draining. The Cu can be electrochemically deposited on the electrode 250 using the current circuit 252 and the voltage source 254. The M2 molecule can be removed from the second chamber 246 to the chamber 202 for use in the second state of the next cycle(s). Example 2

[0083] In at least one embodiment described in Fig. 5, a non-limiting exemplary system 300 may include a chamber 302 having an opening 304 configured as an air inlet. The chamber 302 may include a solid amine-functionalized sorbent 320. The system 300 may have one or more states, steps, or stages. In the first state, the CO2 from the air entering the chamber 302 is bound to the amine of the sorbent 320, and air with a lower CO2 concentration exits via an opening 306 configured as an air outlet. In the first state, the air in the chamber 302 may be passed through the solid amine-functionalized sorbent 320 until a desired CO2 concentration is reached.

[0084] In the second state, stage, or step, the external air flow is stopped, and CO2 is stripped from the sorbent and removed from the system 300. For the purposes of stripping, the sorbent 320 in the chamber 302 may be flooded with a first solution 340 containing the molecule M1, which may be a metal ion(s). The metal ion(s) M1 may favorably bind to the amine groups in the solid sorbent 320, displacing the bound CO2 into the closed sorbent chamber 302. Thus, the CO2 may be stripped from the solid sorbent 320 with the metal ion(s) M1 in the first solution 340. The displaced CO2 is then removed from the chamber 302 for subsequent storage or use. Removal may be accomplished by venting.Once the CO2 is removed from the chamber 302, the first solution 340 is removed from the chamber 302, for example by draining, pumping, suction, or the like.

[0085] In the system of Fig. 5, the one or more mechanical articles described above, such as the centrifuge or a system or a plurality of interconnected centrifuge devices, may be used in the second state according to the principles described above.

[0086] In a third state, the first solution 340 may be replaced by a second solution 341 containing a molecule M2 designed to bind strongly to the metal ion(s) M1 and strip the metal ion(s) M1 from the solid sorbent 320. As a non-limiting example, M2 may include ethylenediamine (EDA) or another appropriately selected small molecular amine. Once the metal ions M1 have reacted with M2, an M1-M2 complex is formed in the second solution 341, which is then removed from the chamber 302. The original state of the solid sorbent 320 is thus restored, and the sorbent 320 can be used to sorb CO2 in the next cycle. The solid sorbent 320 is thus regenerated via the second solution 341, not an EMAR or an electrochemical cell.

[0087] In system 300, an electrochemical cell 330 may be used to regenerate M1, M2, or both. The electrochemical cell 330 may include a membrane 342 separating two chambers 344 (cathode chamber), 346 (anode chamber), each having an electrode 348 (cathode), 350 (anode). The electrodes may be connected to a voltage source 354 via an electrical circuit 352. After removal from the chamber 302, the second solution 341, which includes the M1-M2 complex(es), may then be passed through the electrochemical cell 330, where the metal ions are electrochemically removed from the second solution 341. The removal may be accomplished by electrolytic deposition or inclusion, for example, electrochemical deposition of Cu onto a metallic Cu electrode, or Ag inclusion in a layered oxide cathode 348. The removal of the metal ions regenerates the initial state of the second solution 341.The anode chamber 346 may include a symmetrical anode 350, wherein M1 may be stripped from the anode into the anode chamber 346, thereby creating the source of metal ions M1 for the first solution 340.

[0088] Disclosed herein is a method for reducing CO2 in air or the atmosphere. The method may include direct air capture (DAC). The method may include using one or more of the methods disclosed herein. The method may include providing a chamber containing a solid CO2 sorbent. The method may include passing air (initial or supplied air) through the chamber with the solid sorbent. The passing of air may occur until a predetermined level of saturation is reached. The method may include releasing air from the chamber having a lower CO2 concentration than the initial CO2 concentration in the supplied air.

[0089] The method may further include providing an exchange liquid, a transfer fluid, or a transfer solution into the chamber to regenerate the sorbent once the sorbent is saturated to a desired or predetermined level. Sorbent regeneration may include stripping the CO2 from the solid sorbent to a component M2 present in the exchange fluid. The method may include stripping the CO2 sorbed on the solid sorbent from the sorbent and binding it with M2 within the chamber. The method may include removing the exchange fluid containing the M2-CO2 from the chamber. The removal may be to an electrochemical cell to regenerate M2 and release CO2.

[0090] The method may include the use of mechanical energy and / or a device to regenerate the solid sorbent. The method may utilize one or more centrifuges, each enclosing the solid CO2 sorbent within its body. The method may include the use of one or more subsets or groups of centrifuges operated in staggered fashion. The method may include providing the exchange fluid within the centrifuge, rapidly rotating the centrifuge to force the exchange fluid through the centrifuge body such that the exchange fluid, including the element having a preferential affinity for CO2, binds to the CO2 retained within the solid sorbent body. The method may include expelling the exchange fluid with bound CO2 from the centrifuge, the system, or both.

[0091] The method may include using a subset or group of centrifuges, each subset or group being operated for one cycle. The cycle may include the first, second, third states, or a combination thereof. After a first cycle using the first subset is completed, the mechanical rotational energy is transferred to the second subset via a mechanical linkage. The method may include using a second subset for a second cycle. Subsequently, the method may include using the mechanical energy of the second subset to continue regenerating the solid sorbent with either the first subset or a different subset of centrifuges.

[0092] The process may include regenerating M2 using the cell's voltage and chemistry, such as metal ions from the electrodes, which are exchanged with the CO2 in the cell's cathode chamber. The process may include releasing the dislodged CO2 from the cell. The release may be via a separate tank. The process may include providing the M2-metal ion composition in the cell's anode chamber to dislodge the M2 molecule from the M2-metal ion composition. The dislodgement may be accomplished by electroplating, using the electrode. The process may include reusing the original M2 in the next sorbent regeneration cycle in the chamber.

[0093] The method may include repeating the sorption and desorption cycle within the chamber by repeatedly flooding the chamber with the exchange fluid(s) and draining the exchange fluid(s) from the chamber. The repetition may occur once, twice, three times, or multiple times, for predetermined periods of time.

[0094] Sorbent regeneration may include providing more than one exchange fluid or solution. The more than one fluid may be provided individually, sequentially, or in sequence. The method may include providing an exchange fluid having one or more M1 molecules that bind to the amine present in the solid sorbent and dislodge CO2 from the solid sorbent. The method may include removing the displaced, dislodged, or stripped CO2 from the chamber. The method may then include providing a second exchange fluid in the chamber. The first and second exchange fluids may differ in composition, volume, and / or other property.The second exchange fluid may include molecule(s) M2 that bind more strongly to the molecule(s) M1 than to the sorbent, stripping M1 from the solid sorbent and forming a complex(es) M1-M2.

[0095] The method may further include providing the M1-M2 complex(es) in an electrochemical cell to isolate M1, M2, or both. Isolation may be accomplished via electrolytic deposition or otherwise, using cell chemistry, voltage, or both. The method may include recycling the original M1, M2, or both to the chamber for the next sorbent regeneration cycle.

[0096] The method may include providing more than one chamber, such as 2, 3, 4, 5, 6, 7, 8, 9, 10, or more chambers, each containing a solid sorbent. The method may include sorbing and desorbing CO2 from the solid sorbent in each chamber one or more times before providing the M1-M2 and / or M2-CO2 complex(es) in the electrochemical cell to isolate M1, M2.

[0097] Although exemplary embodiments are described above, these embodiments are not intended to describe all possible forms encompassed by the claims. The language used in the specification is for the purpose of description rather than limitation, and it is understood that various changes may be made without departing from the spirit and scope of the disclosure. As previously described, the features of various embodiments may be combined to form further embodiments of the invention that may not be explicitly described or illustrated.Although various embodiments may have been described as providing advantages with respect to one or more desired features or being preferred over other prior art embodiments or implementations, those skilled in the art will recognize that one or more features or characteristics may be compromised to achieve desired overall system attributes, depending on the specific application and implementation. These attributes may include, but are not limited to, cost, strength, durability, lifetime cost, marketability, appearance, packaging, size, maintainability, weight, manufacturability, ease of assembly, etc.As such, to the extent that embodiments are described as less desirable than other embodiments or prior art implementations with respect to one or more features, these embodiments are not outside the scope of the disclosure and may be desirable for certain applications. QUOTES CONTAINED IN THE DESCRIPTION

[0000] This list of documents submitted by the applicant was generated automatically and is included solely for the convenience of the reader. This list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions. Cited patent literature

[0000] US 18 / 162,326

[0001]

Claims

[1] Carbon dioxide (CO2) direct air capture (DAC) system, which includes: a centrifuge with a cylindrical body containing a solid CO2 sorbent; an injector including an exchange fluid path into the centrifuge; and an exchange fluid that includes a chemical component with a preferential affinity to CO2, wherein the system has a cycle including: a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent and a second state of regenerating the solid CO2 sorbent by injecting the exchange fluid from the injector into the cylindrical body, rapidly rotating the cylindrical body to suck the exchange fluid through a volume of the solid CO2 sorbent, whereby CO2 is released from the solid CO2 sorbent and the released CO2 is bound to the chemical component. [2] The system of claim 1, wherein the cycle further includes a third state of regenerating the chemical component by stripping CO2 from the chemical component and releasing the CO2 from the system. [3] The system of claim 1, wherein the chemical component includes an amine dissolved in an aqueous solution. [4] The system of claim 2, wherein a temperature of the solid CO2 sorbent is maintained at a constant value throughout the first, second and third states of the cycle. [5] The system of claim 1, wherein the centrifuge further includes a central opening defined by the cylindrical body. [6] The system of claim 5, wherein the injector injects the replacement fluid into the central opening. [7] The system of claim 1, wherein the centrifuge further includes an exchange fluid collection jacket. [8] Carbon dioxide (CO2) direct air capture (DAC) system, which includes: a plurality of centrifuges including a first centrifuge and a second centrifuge connected by a mechanical linkage, the first and second centrifuges each containing a solid CO2 sorbent and configured to operate in a staggered manner to remove an exchange fluid from the system after the exchange fluid binds CO2. [9] The system of claim 8, wherein the first and second centrifuges include the same solid CO2 sorbent. [10] The system of claim 8, wherein each of the first and second centrifuges includes a cylindrical body containing the solid CO2 sorbent. [11] The system of claim 8, wherein the mechanical connection is a flywheel. [12] The system of claim 8, wherein the staging includes operating the first centrifuge for one cycle and then mechanically transferring mechanical energy of the first centrifuge to the second centrifuge. [13] The system of claim 12, wherein the cycle includes: a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent and a second state of regenerating the solid CO2 sorbent by injecting the exchange fluid containing a chemical component having a preferential affinity to CO2 into the first centrifuge, rapidly rotating the centrifuge to draw the exchange fluid through a volume of the solid CO2 sorbent, dislodging CO2 and binding the dislodged CO2 to the chemical component. [14] The system of claim 8, wherein the solid CO2 sorbent includes an amine dissolved in an aqueous solution. [15] The system of claim 12, wherein a temperature of the solid sorbent is maintained at a constant value throughout the first and second states of the cycle. [16] Carbon dioxide (CO2) direct air capture (DAC) system, which includes: a first group of centrifuges, each having a body containing a solid CO2 sorbent; a second group of centrifuges, each having a body containing a solid CO2 sorbent; a mechanical connection connecting the first group to the second group; an injector designed to provide an exchange fluid in each centrifuge; and the exchange fluid, which includes a chemical component with a preferential affinity to CO2, wherein the system comprises a cycle of CO2 sorption on the solid CO2 sorbent and CO2 desorption from the exchange fluid in the first group of centrifuges, followed by the cycle in the second group of centrifuges. [17] The system of claim 16, wherein the cycle includes: a first state of sorbing CO2 from incoming air onto the solid CO2 sorbent and a second state of regenerating the sorbent by injecting the exchange fluid into the first group, rapidly rotating the first group to suck the exchange fluid through a volume of the sorbent in each centrifuge, whereby CO2 is released from the solid CO2 sorbent and the released CO2 is bound to the chemical component. [18] The system of claim 16, wherein mechanical energy of the first group of centrifuges is mechanically transferred to the second group of centrifuges via the mechanical connection. [19] The system of claim 16, wherein the mechanical connection is a flywheel. [20] The system of claim 16, wherein the centrifuges in the first group of centrifuges have a cylindrical body.

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