Systems and methods for resource-efficient carbon dioxide capture

Abstract

A system for recovering sorbent gas from a sorbent is disclosed, including a regeneration vessel enclosing a sorbent having sorbent gas, a liquid water supply heated to a first temperature, and a heat pump with a condenser. The heat pump is also connected to the water supply. Heat is removed from the condenser and used to heat the water supply to the first temperature. The system includes a compressor connected to the condenser. The sorbent in the vessel is contacted with water vapor at the first temperature. When the water vapor contacts the sorbent material, the sorbent gas is released, forming a mixture containing sorbent gas and water vapor, and the pressure increases. The vapor mixture is removed and cooled by the condenser. A portion is condensed to water and returned to the supply. The remaining mixture is compressed into a product gas.

Description

Technical Field

[0001] Related Applications

[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63 / 123,219, entitled "Systems and Methods for Energy-Efficient Carbon Dioxide Capture," filed on December 9, 2020, the entire disclosure of which is incorporated herein by reference.

[0002]

[0002] Aspects of this document generally relate to the capture of carbon dioxide.

Background Art

[0003]

[0003] The need for technologies to remove carbon dioxide from ambient air is well established. To avoid the imminent climate change crisis, in addition to conservation, carbon reduction processes, and on-site capture efforts, it is necessary to remove a significant amount of carbon dioxide from the atmosphere. Nevertheless, these technologies are still new, and the operation of initial air capture processes requires a large amount of energy. Since carbon dioxide in ambient air is very dilute, carbon dioxide recovery devices in the atmosphere can quickly exceed a stringent energy budget for sucking in and processing large amounts of air.

[0004]

[0004] Due to the low concentration of carbon dioxide in the atmosphere, it is difficult to capture carbon dioxide from the atmosphere. Despite the fact that the theoretically minimum energy requirement for removing carbon dioxide from air is very small (about 22 kJ / mol), most actual processes involve significant inefficiencies, making it difficult to operate close to the theoretical optimum value. Furthermore, the energy required for purifying and compressing the product stream also becomes substantial.

[0005]

[0005] Efficient purification and compression of the product flow are crucial for the widespread adoption of new carbon capture technologies. Large-scale industrial applications need to be pipeline-compatible or well-prepared at high pressures (i.e., above supercritical pressure) with extremely low oxygen and water content. Using conventional methods and systems, the energy requirements for these pressures and purities are prohibitive for most applications. [Overview of the project] [Means for solving the problem]

[0006]

[0006] According to one embodiment, a system for recovering an adsorbent gas from an adsorbent material includes a regeneration container having an opening and configured to enclose an adsorbent structure that has been physically moved through the opening of the regeneration container, the adsorbent structure comprising an adsorbent material on which the adsorbent gas has been adsorbed. The system also includes a liquid water supply device which is connected to the regeneration container in communication with the regeneration container and heated to a first temperature to produce steam, and at least one heat pump. Each of the at least one heat pumps includes at least one closed fluid circuit, at least one heat pump condenser, at least one heat pump evaporator, at least one heat pump pressure reducer, at least one refrigerant, and at least one heat pump compressor. Each closed fluid circuit includes one of the at least one heat pump condensers, one of the at least one heat pump evaporators, one of the at least one refrigerant, one of the at least one heat pump pressure reducer, and one of the at least one heat pump compressor. The system includes a condenser that is movably connected to a regeneration vessel and also movably connected to a liquid water supply device via a liquid pump, and is thermally in contact with a first closed fluid circuit of at least one heat pump. The first closed fluid circuit is also thermally in contact with a liquid water supply device such that heat is removed from the condenser at a second temperature lower than a first temperature and supplied to the liquid water supply device by the first closed fluid circuit at the first temperature. The system also includes a first compressor movably coupled to the condenser. The sorbent structure in the regeneration vessel is in fluid contact with water vapor from the liquid water supply device at the first temperature after the regeneration vessel has been evacuated to a total pressure lower than the pressure corresponding to the saturated vapor pressure of water at the first temperature. When the water vapor comes into contact with the sorbent material, some of the sorbent gas is released, forming a vapor mixture containing the sorbent gas and water vapor, and the total pressure becomes higher than the triple point pressure of the sorbent. The steam mixture is removed from the regeneration vessel and cooled by a condenser, where some of the water vapor in the steam mixture condenses into liquid water, which is then returned to the liquid water supply by a liquid pump. The remainder of the steam mixture is compressed by a first compressor into a first sorbent product gas. The sorbent gas contains carbon dioxide. At least one heat pump further includes a second closed fluid circuit and a third closed fluid circuit.The first sorbent product gas is thermally in contact with the heat pump evaporator of a second closed fluid circuit of at least one heat pump. The second closed fluid circuit extracts heat from the first sorbent product gas at a third temperature, which is lower than the second temperature and below the melting point of water, resulting in the second sorbent product gas and solid water at the third temperature. The heat extracted by the second closed fluid circuit is supplied by the second closed fluid circuit to a liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second and first temperatures. The second sorbent product gas is thermally in contact with the heat pump evaporator of a third closed fluid circuit of at least one heat pump. The third closed fluid circuit extracts heat from the second sorbent product gas at a fifth temperature, which is lower than the third temperature and below the boiling point of the sorbent, resulting in the liquefied sorbent and volatile gas at the fifth temperature.

[0007]

[0007] A particular embodiment may have one or more of the following features: The first closed fluid circuit and the second closed fluid circuit may belong to the same heat pump. The first closed fluid circuit, the second closed fluid circuit, and / or the third closed fluid circuit may belong to the same heat pump. The adsorbent material may be solid. The adsorbent material may include at least one of ion exchange resins, functionalized polymers, activated carbon, carbonates, phosphates, materials containing amine groups, materials containing ammonium groups, and materials containing both amine and ammonium groups. The adsorbent gas may be removed from the adsorbent by at least one of temperature swings, pressure swings, and moisture swings. The first temperature may be between 40°C and 120°C. The second temperature may be between 0°C and 40°C. The third temperature may be between 0°C and -56°C. At least a portion of the solid water may be melted and transferred to a liquid water supply device. The solid water may be melted using ambient heat. Solid water can be melted using heat provided by at least one of the heat pumps. The volatile gas may include at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The third temperature may be selected to be sufficiently low such that the concentration of water in the second sorbent product gas at the third temperature is lower than the water solubility concentration of the liquefied sorbent at the fifth temperature. The system may further include a mechanical pump configured to receive the liquefied sorbent and further increase the pressure of the liquefied sorbent. The final pressure of the liquefied sorbent may be at least equal to the supercritical pressure of carbon dioxide. The water condensed as liquid water at the second temperature by the condenser may first be heated by ambient heat to a sixth temperature near or below the ambient temperature before being returned to the liquid water supply device. The first temperature may be raised such that the temperature difference between the water vapor and the sorbent structure is minimized during heating.

[0008]

[0008] According to another aspect of the present disclosure, a system for recovering an adsorbent gas from an adsorbent material includes a regeneration container configured to enclose an adsorbent structure, which includes an adsorbent material on which the adsorbent gas has been adsorbed, and a liquid water supply device connected movably to the regeneration container and heated to a first temperature to produce steam. The system also includes at least one heat pump and a condenser connected movably to the regeneration container and also connected movably to the liquid water supply device via the liquid pump. The condenser is in thermal contact with a first heat pump of at least one heat pump. The heat pump is also in thermal contact with the liquid water supply device so that heat is removed from the condenser at a second temperature lower than the first temperature and supplied to the liquid water supply device at the first temperature by the first heat pump. The system also includes a first compressor connected movably to the condenser. The sorbent structure in the regeneration container is placed in fluid contact with steam from a liquid water supply device at a first temperature after the regeneration container has been evacuated to a total pressure lower than the saturated vapor pressure of water at a first temperature. When the steam comes into contact with the sorbent material, some of the sorbent gas is released, forming a steam mixture containing the sorbent gas and steam, and the total pressure becomes higher than the triple point pressure of the sorbent. The steam mixture is removed from the regeneration container and cooled by a condenser, where some of the steam in the steam mixture condenses into liquid water, which is then returned to the liquid water supply device by a liquid pump. The remainder of the steam mixture is compressed into a first sorbent product gas by a first compressor.

[0009]

[0009] A particular embodiment may have one or more of the following features: The first sorbate product gas may be in thermal contact with a second heat pump of at least one heat pump. The second heat pump extracts heat from the first sorbate product gas at a third temperature which may be lower than the second temperature and lower than the melting point of water, thereby obtaining the second sorbate product gas and solid water at the third temperature. The heat extracted by the second heat pump of at least one heat pump may be supplied by the second pump to a liquid water supply device at a first temperature and to one of the first heat pumps at a fourth temperature between the second and first temperatures. The second sorbate product gas may be in thermal contact with a third heat pump of at least one heat pump. A third heat pump extracts heat from the second sorbent product gas at a fifth temperature which may be lower than the third temperature and also lower than the boiling point of the sorbent, thereby potentially yielding a liquefied sorbent and volatile gas at the fifth temperature. The first and second heat pumps may be the same heat pump. The first, second, and third heat pumps may all be the same heat pump. The regeneration container may include openings that allow the sorbent structure to move physically when transitioning between the capture of the sorbent and the release of the sorbent for recovery. The sorbent may contain carbon dioxide. At least one heat pump can operate as one of a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator. Each of the at least one heat pumps may include at least one closed fluid circuit, at least one heat pump condenser, at least one heat pump evaporator, at least one heat pump pressure reducer, at least one refrigerant, and / or at least one heat pump compressor. Each closed fluid circuit includes at least one heat pump condenser, at least one heat pump evaporator, at least one refrigerant, at least one heat pump pressure reducer, and at least one heat pump compressor.The first adsorbent product gas may be in thermal contact with the heat pump evaporator of a second closed fluid circuit of at least one heat pump. The second closed fluid circuit extracts heat from the first adsorbent product gas at a third temperature which may be lower than the second temperature and lower than the melting point of water, thereby potentially yielding the second adsorbent product gas and solid water at the third temperature. The heat extracted by the second closed fluid circuit can be supplied by the second closed fluid circuit to a liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second and first temperatures. The second adsorbent product gas may be in thermal contact with the heat pump evaporator of a third closed fluid circuit of at least one heat pump. A third closed fluid circuit can extract heat from the second sorbent product gas at a fifth temperature which may be lower than the third temperature and also lower than the boiling point of the sorbent, thereby obtaining the liquefied sorbent and volatile gas at the fifth temperature. The first and second closed fluid circuits may belong to the same heat pump. The first, second, and third closed fluid circuits may belong to the same heat pump. The sorbent material may be solid. The sorbent material may include at least one of ion exchange resins, functionalized polymers, activated carbon, carbonates, phosphates, materials containing amine groups, materials containing ammonium groups, and materials containing both amine and ammonium groups. The sorbent can be removed from the sorbent by at least one of temperature swings, pressure swings, and moisture swings. The first temperature may be between 40°C and 120°C. The second temperature may be between 0°C and 40°C. The third temperature may be between 0°C and -56°C. At least a portion of the solid water can be melted and transferred to a liquid water supply device. The solid water can be melted using ambient heat. The solid water can be melted using heat provided by at least one of the heat pumps. The volatile gas may include at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The fluid may contain 10 mol% or less of highly volatile components. The pressure in the regeneration container while the sorbent structure is exposed to water vapor may be between 520 kPa and 3000 kPa.The third temperature can be selected to be sufficiently low such that the concentration of water in the second sorbate product gas at the third temperature is lower than the water solubility concentration of the liquefied sorbate at the fifth temperature. The system may further include a mechanical pump configured to receive the liquefied sorbate and further increase the pressure of the liquefied sorbate. The final pressure of the liquefied sorbate may be at least equal to the supercritical pressure of carbon dioxide. The water condensed as liquid water at the second temperature by the condenser may first be heated by ambient heat to a sixth temperature near or below the ambient temperature before being returned to the liquid water supply. The steam supplied to the regeneration vessel can pressurize the total pressure of the regeneration vessel and maintain it at or near the saturation vapor pressure. The regeneration vessel may be maintained at a total pressure that is at least 85% of the saturation pressure of water at the first temperature. The fluid connection between the liquid water supply at the first temperature and the regeneration vessel may be intermittently closed so that the released sorbate gas increases the total pressure until it exceeds the saturation vapor pressure of the steam at the first temperature. A portion of the water vapor in contact with the sorbent material can provide heat to the sorbent material by at least one of sensible heat transfer, condensation, absorption, adsorption, and exothermic reactions. A portion of the water vapor may combine with the sorbent gas, and as a result, the total pressure in the regeneration container may be higher than the vapor pressure of the sorbent vapor in equilibrium with the sorbent material. The first temperature can be raised during heating to minimize the temperature difference between the water vapor and the sorbent structure. The system may further include at least one nozzle coupled to a liquid water supply device within the regeneration container. The water vapor may be introduced into the regeneration container as heated liquid water from the liquid water supply device passes through the at least one nozzle and a portion of the heated liquid water expands into water vapor, generating a hot mist containing water vapor and water droplets. The system may further include a second liquid pump in fluid communication with the liquid water supply device and pressurizing the heated liquid water delivered to the at least one nozzle in the regeneration container. The second sorbate product gas may be condensed in a distillation unit that can be thermally contacted with a second heat pump of at least one heat pump, the distillation unit condenses the second sorbate product gas into a liquefied sorbate and a volatile gas.The second sorbent product gas may be condensed in a distillation unit that can be thermally contacted with the heat pump evaporator of the second closed fluid circuit of at least one heat pump, and the distillation unit condenses the second sorbent product gas into a liquefied sorbent and a volatile gas. The system may further include a fourth heat pump from at least one heat pump. The fourth heat pump and the second heat pump may be in intermittent fluid contact with the first sorbent product gas, so that when one of the fourth heat pump and the second heat pump is in fluid contact with the first sorbent product gas, the other of the fourth heat pump and the second heat pump may be isolated from the first sorbent product gas. The fourth heat pump extracts heat from the first sorbent product gas at a third temperature, so that the second sorbent product gas and solid water may be obtained at the third temperature. The system may be configured such that, when one of the fourth heat pump and the second heat pump can be in fluid contact with the first adsorbent product gas, at least a portion of the solid water can be in thermal contact with the other of the fourth heat pump, causing the second heat pump to melt and transfer the solid water to a liquid water supply device. The system may further include a fourth closed fluid circuit of at least one heat pump. The fourth closed fluid circuit and the second closed fluid circuit may be in intermittent fluid contact with the first adsorbent product gas, so that when one of the fourth closed fluid circuit and the second closed fluid circuit is in fluid contact with the first adsorbent product gas, the other of the fourth closed fluid circuit and the second closed fluid circuit can be isolated from the first adsorbent product gas. The fourth closed fluid circuit extracts heat from the first adsorbent product gas at a third temperature, so that a second adsorbent product gas and solid water can be obtained at the third temperature. The system may be configured such that, when one of the fourth closed fluid circuit and the second closed fluid circuit is in fluid contact with the first sorbate product gas, at least a portion of the solid water comes into thermal contact with the other of the fourth closed fluid circuit and the second closed fluid circuit, melts, and is transferred to a liquid water supply device.

[0010]

[0010] According to yet another aspect of the present disclosure, a method for recovering an sorbent gas from an sorbent material includes the step of housing an sorbent structure containing an sorbent material with an sorbent gas sorbed into it in a regeneration container. The method also includes the steps of generating steam by providing heat of a first temperature to a liquid water supply device; reducing the total pressure of the regeneration container to a pressure below the saturated vapor pressure of water at the first temperature; introducing steam at the first temperature into the regeneration container; bringing the steam into fluid contact with the sorbent material to release a portion of the sorbent gas and form a steam mixture containing the sorbent gas and steam; and raising the total pressure in the regeneration container to a pressure above the triple point pressure of the sorbent. The method includes the step of allowing the vapor mixture to exit the regeneration vessel by bringing the vapor mixture into fluid contact with a condenser, which is connected responsively to the regeneration vessel and also responsively to a liquid water supply via a liquid pump, wherein the condenser is in thermal contact with a first heat pump, which is also in thermal contact with the liquid water supply, and the first heat pump is at least one of several heat pumps. The method also includes the steps of using the first heat pump to remove heat from the vapor mixture at a second temperature lower than a first temperature; condensing a portion of the water vapor in the vapor mixture into liquid water; supplying the heat removed from the vapor mixture at the second temperature to the liquid water supply at the first temperature; and using the liquid pump to return the liquid water condensed from the vapor mixture to the liquid water supply. Finally, the method includes compressing the remainder of the vapor mixture using a first compressor, which is connected responsively to the condenser, to form a first sorbent product gas.

[0011]

[0011] A particular embodiment may have one or more of the following features. The method may further include extracting heat from the first sorbent product gas at a third temperature using a second heat pump that is thermally in contact with the first sorbent product gas to obtain the second sorbent product gas and solid water at the third temperature. The third temperature may be lower than the second temperature and may be lower than the melting point of water. The method may further include supplying the heat extracted by the second heat pump of at least one heat pump to one of a liquid water supply device at a first temperature and a first heat pump at a fourth temperature between the second and first temperatures. The method may further include extracting heat from the second sorbent product gas at a fifth temperature using a third heat pump that is thermally in contact with the second sorbent product gas to produce a liquefied sorbent and a volatile gas at the fifth temperature. The fifth temperature may be lower than the third temperature and may be lower than the boiling point of the sorbent. The first and second heat pumps may be the same heat pump. The first, second, and third heat pumps may be the same heat pump. This method may further include physically moving the sorbent structure into the regeneration vessel through the opening of the regeneration vessel before reducing the total pressure of the regeneration vessel. The sorbent may contain carbon dioxide. At least one heat pump can operate as one of a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator. Each of the at least one heat pumps may include at least one closed fluid circuit, at least one heat pump condenser, at least one heat pump evaporator, at least one heat pump pressure reducer, at least one refrigerant, and at least one heat pump compressor. Each closed fluid circuit may include one of at least one heat pump condensers, one of at least one heat pump evaporators, one of at least one refrigerant, one of at least one heat pump pressure reducers, and one of at least one heat pump compressors.This method may include a step of extracting heat from the first sorbent product gas at a third temperature using a second closed fluid circuit of at least one heat pump that is thermally in contact with the first sorbent product gas, thereby obtaining a second sorbent product gas and solid water at the third temperature. The third temperature may be lower than the second temperature and may also be lower than the melting point of water. This method may include supplying the heat extracted by the second closed fluid circuit to one of a liquid water supply device at the first temperature and a first closed fluid circuit downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second and first temperatures. This method may include a step of extracting heat from the second sorbent product gas at a fifth temperature using a third closed fluid circuit of at least one heat pump that is thermally in contact with the second sorbent product gas, thereby producing a liquefied sorbent and a volatile gas at the fifth temperature. The fifth temperature may be lower than the third temperature and may also be lower than the boiling point of the sorbent. The first closed fluid circuit and the second closed fluid circuit may belong to the same heat pump among at least one heat pump. The first closed fluid circuit, the second closed fluid circuit, and the third closed fluid circuit may belong to the same heat pump among at least one heat pump. The adsorbent material may be solid. The adsorbent material may include at least one of ion exchange resins, functionalized polymers, activated carbon, carbonates, phosphates, materials containing amine groups, materials containing ammonium groups, and materials containing both amine and ammonium groups. The adsorbent can be removed from the adsorbent by at least one of temperature swings, pressure swings, and moisture swings. The first temperature may be between 40°C and 120°C. The second temperature may be between 0°C and 40°C. The third temperature may be between 0°C and -56°C. This method may include the steps of melting at least a portion of solid water and adding the water to a liquid water supply device. The solid water can be melted using ambient heat. Solid water can be melted using heat provided by at least one of the heat pumps. The volatile gas may include at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide.The fluid may contain less than 10 mol% of highly volatile components. The pressure in the regeneration vessel while the sorbent structure is exposed to water vapor may be between 520 kPa and 3000 kPa. The third temperature may be selected to be sufficiently low such that the concentration of water in the second sorbent product gas at the third temperature is lower than the water solubility concentration of the liquefied sorbent at the fifth temperature. This method may include increasing the pressure of the liquefied sorbent using a mechanical pump configured to receive the liquefied sorbent. The final pressure of the liquefied sorbent may be at least equal to the supercritical pressure of carbon dioxide. This method may include heating the condensed liquid water from the vapor mixture to a sixth temperature near or below the ambient temperature using ambient heat before returning it to the liquid water supply device. The water vapor supplied to the regeneration vessel can pressurize the total pressure of the regeneration vessel and maintain it at or near the saturation vapor pressure. The regeneration vessel may be maintained at a total pressure that is at least 85% of the saturation pressure of water at the first temperature. This method may include intermittently closing the fluid connection between a liquid water supply device at a first temperature and a regeneration container, thereby increasing the total pressure of the regeneration container to exceed the saturated vapor pressure of water vapor at the first temperature through the released sorbent gas. A portion of the water vapor in contact with the sorbent material may provide heat to the sorbent material through at least one of sensible heat transfer, condensation, absorption, adsorption, and exothermic reactions. A portion of the water vapor may combine with the sorbent gas, resulting in the total pressure of the regeneration container potentially exceeding the vapor pressure of the sorbent vapor in equilibrium with the sorbent material. The first temperature may be increased such that the temperature difference between the water vapor and the sorbent structure is minimized during heating. This method may include a step of using a volatile gas at a fifth temperature as a heat sink. This method may include a step of using a volatile gas at a fifth temperature to produce a useful effect. This method may include a step of using a volatile gas at a fifth temperature as a source of drying gas as part of a drying process. This method may include a step of using a volatile gas at a fifth temperature as a source of drying gas for the operation of a pneumatic device.Generating steam involves passing heated liquid water from a liquid water supply device through at least one nozzle located in a regeneration vessel and connected to the liquid water supply device in a manner that allows communication. A portion of the heated liquid water may expand into steam in the regeneration vessel, generating a hot mist containing steam and water droplets. This method may also include pressurizing the heated liquid water delivered to at least one nozzle in the regeneration vessel using a second liquid pump in fluid communication with the liquid water supply device. This method may also include condensing a second sorbent product gas in a distillation unit that can be thermally contacted with a second heat pump, the distillation unit condensing the second sorbent product gas into a liquefied sorbent and a volatile gas. This method may also include condensing a second sorbent product gas in a distillation unit that is thermally contacted with a heat pump evaporator of a second closed fluid circuit of at least one heat pump, the distillation unit condensing the second sorbent product gas into a liquefied sorbent and a volatile gas. This method may include intermittently arranging a second heat pump and a fourth heat pump so as to be in fluid contact with the first sorbate product gas, such that when one of the fourth heat pump and the second heat pump is in fluid contact with the first sorbate product gas, the other of the fourth heat pump and the second heat pump is isolated from the first sorbate product gas. This method may include using the fourth heat pump to extract heat from the first sorbate product gas at a third temperature to obtain the second sorbate product gas and solid water at the third temperature. This method may include melting at least a portion of the solid water by thermal contact with one of the fourth heat pump and the second heat pump, while the other of the fourth heat pump and the second heat pump is in fluid contact with the first sorbate product gas. This method may also include transferring liquid water from the portion of the molten solid water to a liquid water supply device.This method may include intermittently arranging a second heat pump and a fourth closed fluid circuit so as to be in fluid contact with the first adsorbent product gas, such that when one of the fourth and second closed fluid circuits is in fluid contact with the first adsorbent product gas, the other of the fourth and second closed fluid circuits is isolated from the first adsorbent product gas. This method may include using the fourth closed fluid circuit to extract heat from the first adsorbent product gas at a third temperature to obtain the second adsorbent product gas and solid water at the third temperature. This method may include melting at least a portion of the solid water that is in thermal contact with one of the fourth and second closed fluid circuits, while the other of the fourth and second closed fluid circuits is in fluid contact with the first adsorbent product gas. This method may also include transferring liquid water from the portion of the molten solid water to a liquid water supply device.

[0012]

[0012] The aspects and applications of the disclosure presented herein are illustrated by the following drawings and detailed description. Unless otherwise specified, the words and phrases in this specification and claims are intended to have meanings that are plain, ordinary, and familiar to those skilled in the art. The inventors are well aware that they can be their own lexicographers if necessary. The inventors, as their own lexicographers, explicitly choose to use only the obvious and ordinary meanings of terms in the specification and claims unless otherwise specified, and further explicitly indicate any “special” definitions of those terms and explain how they differ from the obvious and ordinary meanings. Where there is no such explicit expression of intent to apply a “special” definition, it is the inventors’ intention and desire that the simple, obvious, and ordinary meanings of the terms apply to the interpretation of the specification and claims.

[0013]

[0013] The inventors are also aware of the ordinary principles of English grammar. Therefore, where a noun, term, or phrase is intended to be further characterized, specified, or narrowed down in any way, then such a noun, term, or phrase will be explicitly given additional adjectives, descriptive terms, or other modifiers in accordance with the ordinary rules of English grammar. Where such adjectives, descriptive terms, or modifiers are not used, such a noun, term, or phrase is intended to be given an ordinary English meaning that is obvious to those skilled in the art of the subject.

[0014]

[0014] Furthermore, the inventors are well aware of the standards and application of the special provisions of § 112(f) of the United States Patent Act. Therefore, the use of the terms “function,” “means,” or “steps” in the detailed description or the description of the drawings or in the claims is not intended to indicate any desire to invoke the special provisions of § 112(f) of the United States Patent Act in any way to define the invention. On the contrary, if the provisions of § 112(f) of the United States Patent Act are applicable, they are required to be invoked to define the invention, and the claims will specifically and explicitly include the exact phrases “means” or “steps,” and also include the word “function” (i.e., “means for performing the function of [insert function]”), and such phrases will not refer to any structures, materials, or actions supporting that function. Therefore, even if the claims include “means for performing the function of ~” or “steps for performing the function of ~,” if the claims also include any structure, material, or act supporting that means or step, or performing the described function, then it is the inventor’s clear intention not to invoke Section 112(f) of the U.S. Patent Act. Furthermore, even if Section 112(f) of the U.S. Patent Act is invoked to define the claimed embodiments, these embodiments are not intended to be limited to the specific structures, materials, or acts described in the preferred embodiments. However, they also include any well-known equivalent structures, materials, or acts, currently or hereafter developed, for performing the claimed function or the function described in the claims, as described in alternative embodiments or forms of this disclosure.

[0015]

[0015] The foregoing and other embodiments, features, and advantages will be apparent to those skilled in the art from the description and drawings, as well as the claims.

[0016]

[0016] The present disclosure will be described below in conjunction with the attached drawings, and the same reference numerals indicate the same elements. [Brief explanation of the drawing]

[0017] [Figure 1]

[0017] This is a schematic diagram of the sorbed material recovery system and method. [Figure 2]

[0018] This is a schematic diagram of another embodiment of an sorbent recovery system comprising at least three heat pumps. [Figure 3]

[0019] This is a schematic diagram of different embodiments of an sorbent recovery system equipped with at least three heat pumps. [Figure 4]

[0020] This is a schematic diagram of one embodiment of an sorbent recovery system equipped with a single heat pump. [Figure 5]

[0021] This is a schematic diagram of another embodiment of an sorbent recovery system equipped with a single heat pump. [Figure 6]

[0022] This is a schematic diagram of one embodiment of an sorbate recovery system comprising two heat pumps and a distillation unit. [Modes for carrying out the invention]

[0018]

[0023] This disclosure, its embodiments, and implementations are not limited to any specific type of material, component, method, or other example disclosed herein. Many additional types of material, components, methods, and procedures known in the art are intended for use in any particular implementation of this disclosure. Thus, for example, while a particular implementation is disclosed, such implementation and implementation components may include any components, models, types, materials, versions, quantities, etc., known in the art with respect to such systems and implementation components, as long as they are consistent with the intended operation.

[0019]

[0024] The terms "exemplary", "example", or its various forms are used herein to mean serving as an example, instance, or illustration. Any aspect or design described herein as "exemplary" or "example" should not necessarily be construed as more preferable or advantageous than other aspects or designs. Further, examples are provided only for purposes of clarification and understanding, and are not intended to limit or restrict the disclosed subject matter or relevant portions thereof in any way. It should be understood that numerous additional or alternative examples within various ranges could have been presented, but have been omitted for brevity.

[0020]

[0025] The present disclosure includes many embodiments in many different forms, which are shown in the drawings, and the present disclosure should be considered as an exemplification of the principles of the disclosed methods and systems, and specific embodiments are described in detail herein with the understanding that the present disclosure is not intended to limit the broad aspects of the disclosed concepts to the illustrated embodiments.

[0021]

[0026] The need for technologies to remove carbon dioxide from ambient air is well established. To avoid the impending climate change crisis, in addition to conservation, carbon reduction processes, and efforts in on-site capture, it is necessary to remove a significant amount of carbon dioxide from the atmosphere. Nevertheless, these technologies are still new, and the operation of the initial air capture processes requires a large amount of energy. Since carbon dioxide in ambient air is very dilute, carbon dioxide recovery devices in the atmosphere can quickly exceed a severe energy budget for sucking in and processing large amounts of air.

[0022]

[0027] Due to the low concentration of carbon dioxide in the atmosphere, it is difficult to capture carbon dioxide from the atmosphere. Despite the fact that the theoretically minimum energy requirement for removing carbon dioxide from air is very small (about 22 kJ / mol), most actual processes involve significant inefficiencies, making it difficult to operate close to the theoretical optimum. Further, the energy required for purification and compression of the product stream also becomes substantial.

[0023]

[0028] Efficient purification and compression of the generated stream is extremely important for the widespread adoption of new carbon capture technologies. Industrial applications operating on a large scale need to be well-prepared to handle pipelines or to be in a state with extremely low oxygen and water content at high pressures (i.e., above supercritical pressure). Using conventional methods and systems, the energy requirements for these pressures and purities become exorbitant for most applications.

[0024]

[0029] This specification contemplates systems and methods for capturing carbon dioxide from the atmosphere in a resource-efficient manner. Specifically contemplated herein are systems and methods that can efficiently recover carbon dioxide or other sorbent gases from a sorbent and then purify the sorbent to produce a compressed stream of the sorbent gas or a condensed liquid form of the sorbent. The present disclosure describes systems, devices, and processes that combine heat, pressure, and moisture swing approaches to minimize energy consumption and other costs in process design. According to various embodiments, the contemplated systems and methods use steam as a carrier or sweep gas. Some embodiments also use the condensation and evaporation of water as a mechanism for supplying heat to and removing heat from the system while generating all or nearly all of the heat required within the gas compression and purification units via mechanical equipment, and employ separation techniques to produce essentially pure carbon dioxide at high pressure.

[0025]

[0030] As described below, according to various embodiments, both the energy required for heating and the water consumed are substantially recovered, improving overall energy efficiency and reducing the utility requirements of the gas separation. Excess energy (e.g., energy exceeding the energy directly consumed by sorbate desorption) is substantially recovered by cooling and condensing the steam in the product effluent and any additional steam removed from the regeneration vessel by evaporative cooling. The sensible heat and heat of vaporization removed during cooling and condensation are heated using one or more heat pumps and then used to generate steam. In some embodiments, this steam is generated using water that is substantially recovered for reuse. This minimizes the specific energy requirements and water consumption of the process.

[0026]

[0031] Using the systems and methods envisioned herein, it is possible to extract low-grade carbon dioxide from the atmosphere and produce purified liquid carbon dioxide using some of the resources (e.g., energy, water, etc.) consumed by conventional systems and methods. This is made possible by integrating the concept of cascade refrigeration with the purification and pressurization processes, as described below.

[0027]

[0032] Much of the following description is given in the context of systems for extracting carbon dioxide from ambient airflow, but it should be noted that the systems and methods intended herein are also applicable to other sorbents and sorbent gases taken from the atmosphere or elsewhere. For example, some embodiments are adapted to remove carbon dioxide from flue gas or other gases from a mixture.

[0028]

[0033] Generally, sorbition / desorption systems involve one or more changes in process conditions to facilitate the binding of an sorbent to the sorbent in one part of the cycle and the release of the sorbent from the sorbent in another part of the cycle. Process variables that can be changed to alter the behavior of the sorbent from sorbition to desorption or vice versa include changes in temperature, pressure, or the presence of other compounds. For gaseous sorbents, increasing temperature increases the equilibrium partial pressure of the sorbent, thus facilitating its release. Conversely, at a constant temperature, decreasing the partial pressure of the sorbent relative to the sorbent reverses the reaction between the sorbent and the sorbent from sorbition to desorption. Furthermore, the release of the sorbent can be influenced by introducing another chemical substance. This could simply be another sorbent that competitively binds to the sorbent and removes the desired sorbent. Or, the reaction of the sorbent and / or sorbent with the other chemical substance may affect the strength of the binding between the sorbent and the sorbent. This latter situation exists in the case of moisture swing of sorbents, as described in other disclosures and research literature. It is important to note that water swing is not simply caused by water replacing carbon dioxide from the sorbent. The presence of water fundamentally weakens the interaction between the sorbent (e.g., carbon dioxide) and the sorbent, and therefore induces the release of the sorbent. Otherwise, simply exposing the sorbent to ambient conditions would not release the water once it has bound.

[0029]

[0034] Figure 1 is a schematic diagram of a non-limiting example of an efficient sorbent recovery system (hereinafter referred to as the recovery system or system). As shown, the system 100 comprises a regeneration container 108 configured to enclose an sorbent structure 104, a liquid water supply device 110, at least one heat pump 120, a compressor 126, and a condenser 118. In some embodiments, the system 100 may also include a liquid pump 122 and some additional heat source (not shown). Each of these elements will be described in detail below.

[0030]

[0035] The regeneration container 108 is configured to enclose an sorbent structure 104 containing an sorbent material 106 on which the sorbent gas 102 has been sorbed. While this disclosure focuses on non-limiting examples of systems and methods for efficiently recovering carbon dioxide, it should be noted again that the systems and methods contemplated herein can be adapted for use with other sorbent materials targeting other sorbent gases.

[0031]

[0036] The regeneration container 108 encloses the sorbent structure 104 to an extent sufficient to expose it to high temperature and / or reduced pressure in order to release the sorbent gas 102 sorbed from the sorbent material 106. In some embodiments, including non-limiting examples shown in Figures 1 to 6, the regeneration container 108 may be configured to receive the sorbent structure 104, which is physically moved within the container 108 through an opening 154, after the sorbent gas 102 from a desired source such as the atmosphere has been loaded into the sorbent material 106. In some embodiments, the sorbent 102 may be captured by the sorbent structure 104 from the atmosphere carried to the sorbent structure 104 by natural convection, while in other embodiments, the sorbent 102 may be captured from a driven airflow.

[0032]

[0037] In some embodiments, the sorbent material 106 may be a solid material, while in other embodiments, the sorbent 106 may be a liquid held within a solid material so as to be exposed to the ambient atmosphere. Examples of sorbent 106 include, but are not limited to, ion exchange resins, functionalized polymers, activated carbon, carbonates, phosphates, or other materials containing amine groups, ammonium groups, amine groups, and ammonium groups. There are many ways to facilitate the release of the sorbent 102 from the sorbent 106, including, but are not limited to, the use of heat in the regeneration process (i.e., temperature swing), the use of low pressure (i.e., pressure swing), and the addition of moisture (i.e., moisture swing). Important to this approach is that, according to various embodiments, the presence of water 136 does not hinder the release of the sorbent 102. As described above, in some embodiments, the sorbent 102 may be captured from the ambient atmosphere, while in other embodiments, it may be captured from a more specific source, such as the output of a combustion process.

[0033]

[0038] In some embodiments, an sorbent structure 104 containing an sorbent material 106 is positioned in fluid contact with the atmosphere or ambient airflow, resulting in the sorbent substance 102, which is one or more components, being sorbed onto the sorbent 106. Once filled with the sorbent substance 102, the sorbent structure 104 is housed in a stationary regeneration container 108. In some embodiments, the sorbent structure 104 can be separated from the atmosphere by physically moving it into the regeneration container 108. After the sorbent substance 102 has been released and captured, the sorbent structure 104 can be moved out of the container 108 to capture more sorbent substance 102. This is repeated, resulting in intermittent outflow of the desorbed sorbent substance 102. In some embodiments, multiple sorbent structures 104 and regeneration containers 108 can be operated in a staggered order so that the combined outflow flow is provided at a near-steady rate.

[0034]

[0039] As shown in the figure, the liquid water supply device 110 is connected to the regeneration container 108 so as to be able to communicate with it. In some embodiments, this fluid communication does not need to be interrupted, but in other embodiments, it may be controllable via a fluid connection 156 such as a valve, which makes it possible to interrupt the fluid communication between the regeneration container 108 and the liquid water supply device 110, as will be further described below.

[0035]

[0040] System 100 also includes at least one heat pump 120. According to various embodiments, one or more heat pumps 120 operate as one of the following, as known in the Art: a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator. For example, in some embodiments, the heat pump may have one or more closed fluid circuits 142, each circuit 142 having one or more refrigerants 150, one or more evaporators 146, one or more compressors 152, one or more condensers 144, and one or more pressure reducers 148. As illustrated, the heat pump 120 interacts with other components of System 100, either centered (e.g., System 100 in Figure 1) or via a heat exchanger 160 between a heat pump condenser 144 and a heat pump evaporator 146 (e.g., System 300 in Figure 3). The heat pump (S) 120 may use a refrigerant 150 selected from R-12, R-13, R-22, R-23, R-134a, R-152a, R-E170, R-290, R-502, R-503, R-507, R-508B, R-1234yf, R-404A, R-407A, R-600, R-600a, R-630, R-631, R-717, R-764, and R-744, depending on the various embodiments.

[0036]

[0041] The following is a non-limiting example of a method for efficiently recovering the sorbent gas 102 using the system 100 intended herein. First, an sorbent structure 104 filled with the sorbent gas 102 (e.g., carbon dioxide 103) is placed in a regeneration container 108. See "Circle 1".

[0037]

[0042] A non-limiting example shown in Figure 1 is a simple frame structure covered with an sorbent material 106 placed inside a regeneration container 108. However, those skilled in the art will recognize that the system 100 can be used with any implementation of an sorbent structure 104 having a suitable sorbent material 106, such as the example above, which can be enclosed inside the regeneration container 108 (for example, a structure 104 that can be physically moved within the container 108 when transitioning between capturing and releasing the sorbent material 102 for recovery).

[0038]

[0043] The water in the liquid water supply device 110 is heated so that steam 116 can be supplied to the regeneration container 108. See "Circle 2". As shown, the steam 116 is supplied to the sorbent material 106 in the regeneration container 108 at a first temperature 112. In some embodiments, the first temperature 112 may be between 40°C and 120°C. In some embodiments, the first temperature 112 may be approximately 80°C. Note that the choice of temperature is partly determined by the pressure at which the steam 116 interacts with the sorbent material 106.

[0039]

[0044] As described below, the liquid water supply unit 110 receives heat 124 recovered from the steam 116 as the steam 116 further condenses within the system 100. In some embodiments, the liquid water supply unit 110 may also be heated by an additional heat pump 120 and / or other heat source, if necessary.

[0040]

[0045] In some embodiments, once the sorbent structure 104 is physically moved into the regeneration container 108, the container 108 is filled with other atmospheric gases, particularly volatile gases that need to be further removed for the purification process at the expense of energy. Therefore, it is advantageous to remove as many of these polluting gases (e.g., nitrogen, oxygen, etc.) as possible from the regeneration container 108 before releasing the sorbent gas 102. Furthermore, in some embodiments, the water vapor 116 released in the container 108 may be at atmospheric pressure or below atmospheric pressure, which can be anticipated by evacuating the container 108 before releasing the water vapor 116. Of course, in other embodiments, the water vapor 116 may be at high pressure, as described below.

[0041]

[0046] After container 108 is closed, the total pressure 128 of the regeneration container 108 decreases. See "Circle 3". According to various embodiments, container 108 can be evacuated to a total pressure 128 that is lower than the pressure corresponding to the saturated vapor pressure of water at a first temperature 112 (i.e., the temperature at which steam / vapor is supplied to container 108 in "Circle 4"). Optionally, in some embodiments, sorbent gas 102 and / or steam 116 can be used to clear any undesirable residual gaseous components from the regeneration container 108 before evacuating.

[0042]

[0047] In some embodiments, the total pressure 128 of the vessel 108 can be reduced by a compressor 126 that is in fluid communication with the condenser 118, while in other embodiments, the pressure 128 of the vessel 108 can be reduced using a different compressor (see, for example, the second compressor 616 in Figure 6) or through a different mechanism.

[0043]

[0048] Once the sorbent structure 104, filled with the sorbent material 106, is sealed in the regeneration container 108, it is exposed to heat and moisture via steam / water vapor as part of the regeneration cycle. See "Circle 4". Water vapor 116 is introduced into the container 108 at a first temperature 112, causing the water vapor 116 to come into fluid contact with the sorbent material 106, releasing a portion 130 of the sorbent gas 102 to form a steam mixture 132 containing the sorbent gas 102 and water vapor 116, raising the total pressure 128 inside the regeneration container 108 above the triple point pressure of the sorbent 102. This water vapor causes condensation on the surface, uniformly heating the sorbent 106 inside the container 108, thereby promoting an increase in the partial pressure of the sorbent 102 inside the container 108.

[0044]

[0049] According to various embodiments, a portion of the water vapor 116 in contact with the sorbent 108 provides heat to the sorbent 108 by at least one of sensible heat transfer, condensation, absorption, adsorption, and exothermic reactions. In some embodiments, the water vapor 116 at a first temperature 112 pressurizes the regeneration vessel 108 and maintains it at a pressure corresponding to or near the saturation vapor pressure. In other embodiments, the regeneration vessel 108 is maintained at a pressure of 85% or more of the saturation pressure of water at the first temperature 112. This water vapor 116 expands within the vessel 108 at a lower pressure.

[0045]

[0050] In some embodiments, the liquid water supply device 110 does not require much heat to form steam 116 in a pre-evacuated container 108. When the container 108 is opened and the liquid water supply device 110 is exposed to reduced pressure, steam 116 may spontaneously form in the container.

[0046]

[0051] In some embodiments, the fluid connection 156 between the liquid water supply device 110 and the regeneration container 108 at a first temperature 112 is intermittently closed. This allows the desorbing material 102 to increase the total pressure 128 to a level exceeding the saturated vapor pressure of water vapor 116 at the first temperature 112.

[0047]

[0052] It should be noted that in some embodiments, the water vapor 116 reaching the container 108 is at a first temperature 112, while in some embodiments, the inside of the container 108 may be slightly hotter than the first temperature 112 due to the properties of how water binds with the sorbent material 106. In other embodiments, the sorbent structure 104 and the sorbent material 106 may be at or near the first temperature 112.

[0048]

[0053] In some embodiments, as the system 100 continues to process the sorbent gas 102, the first temperature 112 may rise so as to minimize the temperature difference between the heated steam 116 and the sorbent structure 104. Furthermore, in some embodiments, the pressure 128 in the regeneration container 108 while the sorbent structure 104 is exposed to the steam 116 may be between 520 kPa and 3000 kPa.

[0049]

[0054] According to various embodiments, the steam 116 supplied to the regeneration container 108 pressurizes the total pressure 128 of the regeneration container 108 and maintains it at or near the pressure corresponding to the saturated vapor pressure. In some embodiments, a portion of the steam 116 combines with the sorbent gas 102 such that the total pressure 128 of the regeneration container 108 is higher than the vapor pressure of the sorbent vapor 102 in equilibrium with the sorbent material 106.

[0050]

[0055] In some embodiments, steam 116 at a first temperature 112 is formed in the liquid water supply device 110 and enters the already formed regeneration container 108. In other embodiments, the water may remain in a heated liquid state when it moves to the regeneration container 108, where it rapidly expands to form steam 116, at least partially. As shown in the figures, in some embodiments, the liquid water supply device 110 may be connected to a liquid pump 112 that can pressurize the liquid water in the supply device 110. In other embodiments, heat and moisture may be delivered to the sorbent material 106 in the container 108 in different ways or forms, as described in reference to Figure 6 below.

[0051]

[0056] Next, the vapor mixture 132, containing water vapor 116 and sorbent gas 102, is withdrawn from the regeneration vessel 108. See "Circle 5". In some embodiments, the vapor mixture 132 is removed using an exhaust system such as a condenser and / or vacuum compressor. For example, in one embodiment, a first compressor 126 can be used to withdraw the vapor mixture 132 from the regeneration vessel 108. In another embodiment, a separate device such as a second compressor 616 in Figure 6 may be used. In some embodiments, during the regeneration cycle, some of the water vapor 116 combines with the sorbent gas 102, resulting in a total pressure 128 that is higher than the vapor pressure of the sorbent gas 102 while in equilibrium with the sorbent 108.

[0052]

[0057] In yet another embodiment, the vapor mixture 132 may be swept out of the regeneration container 108 by a sweeping gas introduced into the regeneration container 108, thereby driving out the vapor mixture 132. In some embodiments, additional steam 116 may be used as the sweeping gas, while in other embodiments, a burst of the sorbate gas 102 itself may be used.

[0053]

[0058] In other embodiments, the vapor mixture 132 may be drawn from the regeneration vessel 108 when exposed to a lower temperature condenser 118 fluidically coupled to the regeneration vessel 108. In some embodiments, a continuous flow of the vapor mixture 132 may be drawn from one or more regeneration vessels 108 where the sorbent structure 104 is at various stages of sorbent depletion, allowing for a nearly constant flow of the vapor mixture 132. A continuous flow of the vapor mixture 132 from a single regeneration vessel 108 is complicated by the fact that as the sorbent material 106 lowers the captured sorbent gas 102, the partial pressure of the sorbent gas 102 in the vessel 108 decreases along with the continuous flow of the product.

[0054]

[0059] However, in other embodiments, the fluid communication between the regeneration vessel 108 and the condenser 118 may be intermittent. For example, in some embodiments, a fluid connection 158, such as a valve, can be used to control the fluid communication between the regeneration vessel 108 and the condenser 118. In some cases, it may be more efficient to allow the sorbent structure 104 to remain in the heat and moisture of the water vapor 116 in the regeneration vessel 108, giving it time to release the sorbent gas 102 sorbed onto the sorbent material 106. By closing the fluid connection 156 between the regeneration vessel 108 and the condenser 118, the total pressure 128 may be allowed to increase to a higher level as more sorbent gas 102 is released from the sorbent material 106. These embodiments can be described as operating in pulse mode rather than producing a continuous product flow, releasing bursts of a vapor mixture 132 whose size and spacing can be changed to achieve optimal efficiency (or possibly optimal yield).

[0055]

[0060] After being extracted from the regeneration container 108, the steam mixture 138 enters the condenser 118. As shown in the figure, the condenser 118 is in thermal contact with the heat pump 120, which in turn is in thermal contact with the liquid water supply device 110. The condenser 118 is also connected to communicate with both the liquid water supply device 110 and the compressor 126. In some embodiments, the condenser 118 is coupled to communicate with the liquid water supply device 110 via a liquid pump 122.

[0056]

[0061] According to various embodiments, the heat pump 120 removes heat 124 from the condenser 118 and condenses at least a portion 134 of the water vapor 116 in the steam mixture 138 into liquid water 136. See "Circle 6". This condensation of water produces the remainder 138 of the steam mixture 138, increasing the concentration and partial pressure of the sorbate gas 102. Advantageously, this condensation also reduces the volume of the steam mixture 138, and therefore the amount of work that needs to be done by the compressor 126 is reduced.

[0057]

[0062] In some embodiments, the condenser 118 may be indirect in nature, extracting heat 124 and condensing water vapor 116 through thermal contact with the refrigerant 150 via some other medium (e.g., a housing, coil, etc.). In other embodiments, the condenser 118 may be direct in nature, condensing water vapor 116 through direct contact with cooling liquid water that has been cooled separately by contact with the refrigerant 150. See, for example, the direct condenser 618 in Figure 6.

[0058]

[0063] This process of separating a portion 134 of the water vapor 116 from the adsorbent gas 102 is driven by removing heat 124 from the water vapor 116 to condense it. As shown in the figure, the heat 124 is removed from the condenser 118 at a second temperature 114 (for example, the water vapor 116 reaches a second temperature 114 when it condenses). The second temperature 114 is lower than the first temperature 112. In some embodiments, the second temperature 114 is between 0°C and 40°C. In other embodiments, the second temperature 114 is between 0°C and 15°C. In yet another embodiment, the second temperature 114 is between the melting and boiling points of water.

[0059]

[0064] According to various embodiments, heat 124 is transferred from steam 116 at or near a second temperature 114 to a heat pump evaporator 146. From there, the heat 124 is heated and transferred from the heat pump condenser 144 to a liquid water supply device 110 at or near a first temperature 112, as indicated by "Circle 7". In some embodiments, the first temperature 112 is continuously rising or provided in several temperature increments so that the temperature difference between steam 116 and the sorbent structure 104 is minimized during heating.

[0060]

[0065] As described above, the heat 124 removed from the steam mixture 132 extracted from the regeneration container 108 is reused. The energy required to initially evaporate the liquid water to generate steam for sorbent regeneration contributes significantly to the overall specific energy for producing the sorbent (e.g., carbon dioxide) product. A small portion of this energy is related to the desorption energy of the sorbent gas 102. However, it is desirable to recover as much of the balance of energy used to heat the steam and materials, or present in the steam 116 contents of the regeneration container 108 outflow (i.e., the steam mixture 132), as possible.

[0061]

[0066] The process for doing this involves removing heat from the water vapor 116 in the regeneration effluent, condensing a portion of it outside the regeneration container 10, further re-evaporating a portion of the water condensate inside the regeneration container 108 by vacuum evaporation, and then removing heat to condense a portion of it. The sensible heat removed from the effluent, particularly the heat of vaporization removed by condensing the water in the effluent, is recovered by heat exchange at a temperature lower than the initial water evaporation temperature. This recovered heat is then heated to a higher temperature (e.g., from a second temperature 114 to a first temperature 112) by a heat pump 120 (or, in some embodiments, multiple heat pumps 120) and can be used for regeneration heat and steam generation.

[0062]

[0067] In some embodiments, the heat pump 120 can operate as a simple approximation of the Carnot cycle, while in other embodiments, a more complex and modern cycle can be employed such that the energy consumed in operating the heat pump 120 is far less than the heat 124 recovered and transferred. The recovered and heated heat 124 is used to generate more steam 116 for subsequent regeneration of the sorbent.

[0063]

[0068] The portion 134 of the steam 116 that condenses back into liquid water 136 is returned to the liquid water supply unit 110, where it is reheated at a first temperature 112, using at least partially the heat 124 extracted from the condenser 118 by the heat pump 120. See "Circle 8". As illustrated, in some embodiments, the reused liquid water 136 is transported back to the liquid water supply unit 110 by a liquid pump 122 or similar device that is in fluid communication with both the condenser 118 and the liquid water supply unit 110. According to various embodiments, the heat 124 may be supplied to the liquid water 136 by direct or indirect heat transfer.

[0064]

[0069] While some water loss is unavoidable, reusing this resource improves the efficiency of the intended system 100. In some embodiments, the intended system may be further equipped with a supply of makeup water to compensate for losses due to steam 116 lost when the regeneration container 108 is opened, for example. See, for example, makeup water 612 in Figure 6.

[0065]

[0070] The remainder of the vapor mixture 138 is separated from the portion 134 of the water vapor 116 condensed here by the condenser 118. According to various embodiments, this separation can occur at a nearly constant pressure, and as a result, the condensation of water vapor 116 effectively pressurizes the remaining gas to a level close to the pressure 128 in the regeneration vessel 108. This purified, pressurized, sorbate-rich gas can be removed for further processing, storage, or immediate use. See "Circle 9". In some embodiments, this gas is sent to a first compressor 126 and further pressurized to form a first sorbate product gas 140.

[0066]

[0071] As shown, in some embodiments, the regenerated effluent is compressed after passing through a condenser 118 that performs both purification and compression of the product gas. In other embodiments, the gas can be compressed before heat is removed by the condenser 118, which may be advantageous in certain embodiments where the resource costs associated with mechanical compression are lower than the resource costs associated with heat transfer performed by the condenser 118.

[0067]

[0072] In some embodiments, after the vapor mixture 132 is extracted from the regeneration container 108, everything contained in the container 108 (e.g., the sorbent structure 104) is heated. Furthermore, after the vapor mixture 132 has been substantially removed, residual water may remain in the container 108. In some embodiments, the container 108 may be at least partially evacuated before opening it (e.g., so that the sorbent structure 104 can be physically removed).

[0068]

[0073] When the pressure 128 inside the regeneration container 108 is reduced, the residual liquid water 136 inside the container 108 re-evaporates. This steam 116 is sent to the condenser 118 and reused in the liquid water supply device 110. Furthermore, the re-evaporation effectively cools the device (e.g., the inside of the container 108, the sorbent structure 104, the sorbent material 106, etc.), allowing at least some of its heat 124 to be reused.

[0069]

[0074] Some embodiments of the intended system and method further include additional, resource-efficient mechanisms and procedures for the purification and pressurization of the sorbate 102, which can separate additional water and highly volatile components, while simultaneously making the sorbate 102 more industrially useful. Figures 2–6 are schematic diagrams of non-limiting examples of embodiments of the intended system and method.

[0070]

[0075] Figure 2 is a schematic diagram of a non-limiting example of another embodiment of an efficient sorbate recovery system. This system 200 provides efficient purification and pressurization of the first sorbate product gas 140, which is the product of system 100, and covers the omissions of the non-limiting example shown in Figure 1. As shown in Figure 2, this system 200 can continue the purification and pressurization process using an additional heat pump 120. As previously stated, the systems contemplated herein include systems 100, 200 in Figures 1 and 2, and one or more heat pumps 120 are implemented to reuse heat, water, and volatile gases that would be lost using conventional methods.

[0071]

[0076] As shown in the figure, system 200 includes, in addition to the regeneration container 108, the liquid water supply device 110, condenser 118, first compressor 126, and liquid pump 122 of system 100 in Figure 1, and an additional heat pump 120 is used. Specifically, system 200 utilizes the first heat pump 120a, the second heat pump 120b, and the third heat pump 120c. The role of each of these heat pumps will be described below.

[0072]

[0077] However, before proceeding, it should be noted that each of these heat pumps 120abc can represent multiple heat pumps 120, or one or more heat pumps 120, as well as the single heat pump 120 shown in Figure 1, and at least some of them have multiple closed fluid circuits 142. Heat pumps 120 having multiple closed fluid circuits 142 will be further described in relation to Figures 3 and 4, and in the situation shown in Figure 5 below, a heat pump 120 with a single circuit 142 having multiple pressure drops is shown. Furthermore, the following description of the non-limiting examples shown in Figure 2 will be made in relation to three representative heat pumps 120, which will be considered in terms of their roles without delving deeply into their internal structure (e.g., closed fluid circuits 142, etc.) or the various types of heat pumps 120 that may be used. It should be noted that, according to various embodiments, the heat pump 120 of the intended system can operate in a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator, as is known in the art. The lack of description of some types of heat pumps 120 when describing the internal structures of various non-limiting embodiments in this disclosure should not be construed as limitation. Those skilled in the art will recognize that various heat pumps 120 can be adapted to perform the role of heat pump 120 in this disclosure.

[0073]

[0078] Furthermore, it should be noted that some elements present in system 100, as shown and described in Figure 1, are not present in system 200 in Figure 2. Any omissions should not be interpreted as limitations. Non-limiting examples of system 100 in Figure 1, and a broader set of embodiments producing the same first sorbent product gas 140, including water vapor 116, sorbent gas 102, and other atmospheric gases (including volatile gas 212, described later), can be combined with the elements of system 200, as described below. The omissions of elements shown in Figure 1 are for visual clarity and should not be interpreted as limitations.

[0074]

[0079] A considerable amount of water vapor 116 is removed as it condenses into liquid water 136 while passing through the condenser 118, which is thermally in contact with the first heat pump 120a. However, a sufficient amount of water vapor 116 remains, which may make the product flow unsuitable for many industrial applications. As shown in the figures, the second heat pump 120b is in fluid communication with both the first compressor 126 and the condenser or vessel, which is thermally in contact with the third heat pump 120c, and receives the first sorbent product gas 140 from the first compressor 126 at a second temperature 114 or near it. In the context of this description, drawings and the subsequent claims, it should be noted that the systems contemplated herein and the elements constituting them provide sufficient space for the various vapors and liquids on which the system operates, even if the exact nature of a particular structure is not specified. For example, a person skilled in the art will recognize that, when a second heat pump 120b is described as cooling a first sorbate product gas 140, removing heat 124, and solidifying water vapor, these gases and solids may be contained within or pass through containers, heat exchangers, or condensers, or simply moving within the system 200 in conduits large enough to hold a volume sufficient for the system 200 to operate efficiently. A key aspect, and a fundamental feature of the intended system, is the removal of heat 124 from the intermediate product stream at various points in the recovery, purification, and pressurization processes, according to various embodiments.

[0075]

[0080] As shown, the first sorbate product gas 140 is brought into thermal contact with the second heat pump 120b at approximately a second temperature 114°C and further cooled to a third temperature 202°C, which is lower than the melting point of water but higher than the triple point temperature of carbon dioxide 103 (e.g., sorbate 102). See "Circle 1". As a result, some of the water still present in the first sorbate product gas 140 freezes as solid water 206, which is then separated and removed from the fluid. In some embodiments, the third temperature 202 may be between 0°C and -56°C. As a result of this cooling, the first sorbate product gas 140 is separated into solid water 206 and a second sorbate product gas 204, which is more purified than the first sorbate product gas 140.

[0076]

[0081] According to various embodiments, the heat 124 extracted from the first sorbate product gas 140 at a third temperature 202 can be used to provide heat to the liquid water in the liquid water supply device 110 (at a first temperature 112). See "Circle 2".

[0077]

[0082] Finally, the second sorbate product gas 204 is placed in thermal contact with the third heat pump 120c to extract heat from the second sorbate product gas 204 and further cool to a fifth temperature 208, resulting in a vapor 212 consisting substantially of highly volatile components and a liquid 210 consisting substantially of the sorbate 102 (e.g., carbon dioxide 103). See "Circle 3". According to various embodiments, the fifth temperature 208 is lower than the third temperature 202 and lower than the boiling point of the sorbate 102, resulting in the liquefied sorbate 210 and volatile gas being obtained at the fifth temperature 208.

[0078]

[0083] According to various embodiments, the third temperature 202 may be selected to be sufficiently low such that the concentration of water in the second sorbate product gas 204 at the third temperature 202 is lower than the water solubility concentration in the liquefied sorbate 210 at the fifth temperature 208. In some embodiments, the liquefied sorbate 210 may contain, but is not limited to, nitrogen, oxygen, methane, hydrogen, and carbon monoxide, and may contain 10 mol% or less of highly volatile components. The fifth temperature 208 may be related to the gas-liquid equilibrium of the liquefied sorbate 210 such that more than 90% of the highly volatile components remain in a vapor state (indicated here as volatile gas 212).

[0079]

[0084] As with the other heat pumps 120a and 120b in the intended system 200, according to various embodiments, the heat 124 extracted from the second sorbate product gas 204 at a fifth temperature 208 can be used to provide heat to the liquid water in the liquid water supply device 110 at a first temperature 112. See "Circle 4".

[0080]

[0085] The liquid 210 substantially containing the sorbate 102 may then be pressurized using a mechanical pump 214. See "Circle 5". According to various embodiments, the final pressure 216 of the liquid sorbate 210 is greater than or equal to the supercritical pressure of the sorbate 102 (e.g., carbon dioxide 103). In some embodiments, the portion of the sorbate 102 remaining in the vapor 212 (e.g., carbon dioxide 103) also substantially containing highly volatile components at a third temperature 202 and, after the majority of the sorbate 102 has liquefied, it may be further separated from the volatile gas as a solid (e.g., dry ice), similar to how the residual water is removed by a second heat pump 120b.

[0081]

[0086] In some embodiments, the extracted highly volatile components may be discarded, while in other embodiments, they may be used elsewhere in the system 200. For example, in one embodiment, vapor 212 substantially containing highly volatile components at a fifth temperature 208 can be used as a heat sink 224 for other processes. In another embodiment, this highly volatile component-rich fluid can be depressurized to produce a useful action 226. In yet another embodiment, vapor substantially containing highly volatile components at a fifth temperature 208 can be used as a source of drying gas 228 for the operation of the drying process 230 and / or pneumatic device 232. See "Circle 6".

[0082]

[0087] According to various embodiments, the water 136 extracted by the purification process can be used elsewhere in the regeneration cycle. For example, in some embodiments, a portion of the water separated as solid 206 at a third temperature 202 can be supplied to a liquid water supply unit 110 and heated at a first temperature 112 provided by a first heat pump 120a to produce steam 116. Optionally, the water supplied to the liquid water supply unit 110 may first be heated by ambient heat 218 to a sixth temperature 220 that is close to or below the ambient temperature 222. In other embodiments, the solid water 206 can be melted using ambient heat and at least one of the heat provided by at least one of the multiple heat pumps 120.

[0083]

[0088] As described above, the heat 124 removed during cooling to a second temperature 114 (i.e., condensation of liquid water 136), a third temperature 202 (i.e., freezing of solid water 206), and a fifth temperature 208 (i.e., liquefaction of the adsorbent material 102) can be raised by one or more heat pumps 120 and used as the heat 124 at the first temperature 112 to generate steam 116 for the regeneration of the adsorbent material 106. According to various embodiments, the heat pump 120 can remove the heat 124 at multiple temperatures corresponding to the successive cooling temperatures of the purification process. In some embodiments, the heat pump 120 may comprise multiple closed fluid circuits 142 that may or may not be in thermal contact with each other. In other embodiments, the heat pump 120 may have a single closed fluid circuit 142 with multiple pressure drops corresponding to various successive cooling temperatures of the purification process.

[0084]

[0089] Figures 3 and 4 are schematic diagrams of two non-limiting examples of efficient sorbent recovery systems 300 and 400 utilizing a heat pump 120 having multiple interconnected closed fluid circuits 142. Specifically, Figure 3 is a schematic diagram of a non-limiting example of system 300 having two heat pumps 120c and 120e, one of which has two interconnected closed fluid circuits 142a and 142b. Figure 4 is a schematic diagram of a non-limiting example of system 400 having a single heat pump 120f with three thermally coupled closed fluid circuits 142a, 142b, and 142c.

[0085]

[0090] In the system 300 shown in Figure 3, one of the two heat pumps 120 has a plurality of thermally coupled closed fluid circuits 142. According to various embodiments, a heat pump (e.g., a fifth heat pump 120e) may have two fluid circuits 142, in which case the evaporator 146 of the first fluid circuit 142a operates at or near a second temperature 114, while the evaporator 146 of the second fluid circuit 142b operates at or near a third temperature 202. As shown in Figure 3, these two closed fluid circuits 142a and 142b are configured in a cascaded arrangement such that the condenser 144 of the second closed fluid circuit 142b transfers heat 124 to the evaporator 146 of the first closed fluid circuit 142a at a fourth temperature 302. In other embodiments, these two circuits may reside in separate heat pumps (e.g., the first and second heat pumps 120a, b, etc. in Figure 2) and still be thermally coupled, so that the heat extracted by the second heat pump 120b is supplied by the second pump 120b to either the liquid water supply device 110 at a first temperature 112 or the first heat pump 120a at a fourth temperature 302 between the second temperature 114 and the first temperature 112. In other words, in the non-limiting example of the system 200 shown in Figure 2, the first heat pump 120a and the second heat pump 120b are equivalent as if they were the same heat pump 120. In other embodiments, the heat extracted by the second closed fluid circuit 142b may be supplied by the second closed fluid circuit 142b to the first closed fluid circuit 142a downstream of the heat pump evaporator 146 of the first closed fluid circuit 142a at a fourth temperature 302, which is between the second temperature 114 and the first temperature 112.

[0086]

[0091] This can also be achieved by a heat pump with a single circuit having two pressure drops, where heat is transferred from the steam to the heat pump evaporator at a second temperature or near it, heat is transferred from the steam to the heat pump evaporator at a third temperature or near it, and finally heat is transferred from the heat pump condenser to the liquid water at a first temperature or near it. According to various embodiments, the heat pump has one closed fluid circuit and two levels of pressure reduction, resulting in one evaporator operating at a second temperature or near it and one evaporator operating at a third temperature or near it. A heat pump with three pressure reduction levels will be described with reference to Figure 5 below.

[0087]

[0092] Figure 4 is a schematic diagram of a non-limiting example of an embodiment of an adsorbent recovery system 400 comprising a single heat pump having multiple closed fluid circuits 142 arranged in a cascade for heat transfer. As shown in the figure, this heat pump (e.g., a sixth heat pump 120f) is positioned such that the second adsorbent product gas 204 is in thermal contact with the heat pump evaporator 146 of the third closed fluid circuit 142c of the heat pump 120f. The third closed fluid circuit 142c extracts heat from the second adsorbent product gas 204 at a fifth temperature 208, which is lower than a third temperature 202 and lower than the boiling point of the adsorbent 102, resulting in the production of liquefied adsorbent 102 and volatile gas 212 at the fifth temperature 208. The condenser 144 of the third circuit 142c is thermally coupled to the second circuit 142b upstream of the evaporator 146 of the second circuit 142b and downstream of the condenser 144 of the second circuit 142b. As shown in the figure, heat 124 is transferred from the third circuit 142c to the second circuit 142b at a seventh temperature 402.

[0088]

[0093] Figure 5 is a schematic diagram of a non-limiting example of an embodiment of a system 500 having a single heat pump 120g having a single closed fluid circuit 142. According to some embodiments, the heat pump 120 may have a vapor compression cycle with multiple levels of pressure reduction so that multiple evaporators 146 can operate at or near the continuous cooling temperature. This heat pump 120 (e.g., the seventh heat pump 120g of system 500 in Figure 5) may include one or more closed fluid circuits 142 (e.g., heat pump pressure reducers 148a, 148b, and 148c) that operate at multiple pressure levels and provide a continuous pressure drop so that multiple evaporators 146 can operate at or near the continuous cooling temperature (e.g., a second temperature 114, a third temperature 202, a fifth temperature 208, etc.).

[0089]

[0094] Figure 6 is a schematic diagram of a non-limiting example of another embodiment of the efficient sorbate recovery system 600. Similar to the embodiment shown in Figure 3, this system 600 uses two heat pumps, which can be thought of as a front-end heat pump 620 driving initial steam removal and pressurization, and a back-end heat pump 622 driving additional purification and compression. According to various embodiments, these two subsystems are designed so that their ranges coincide with each other, thereby allowing them to function as repeatable units, and the size of the system 600 can be easily scaled up by having a further number of units work together to recover sorbates from a further number of regeneration vessels 108 and sorbate structures 104.

[0090]

[0095] Many of the features of this system 600 have been described in detail in relation to other embodiments of the system and method to be intended. However, there are many differences. As shown in the illustration, system 600 includes a second compressor 616. Unlike the embodiments described above, this compressor 616 is located upstream of the condenser 618.

[0091]

[0096] First, the void within the sealed regeneration container 108 is filled with enough air to substantially contaminate the sorbed material product. According to some embodiments, the exhaust of container 108 is facilitated by the use of a dedicated vacuum system, such as this compressor 616, which not only removes air pollutants before the introduction of water vapor but can also create an initial vacuum within container 108. This may be advantageous in embodiments where the system 600 is scaled up and it is necessary to coordinate the use of various resources within the system 600.

[0092]

[0097] Another difference lies in the method of delivering heated water to the sorbent material 106 in the container 108. While steam 116 is far more energy-intensive than liquid water 136, the mass of liquid water deployed in the container 108 affects the overall efficiency of the system (e.g., heat and energy waste when moving large amounts of heavy water). According to various embodiments, the system 600 delivers heated water to the sorbent material 106 as hot liquid water pushed out from one or more nozzles 610 by expanding steam.

[0093]

[0098] High-temperature pressurized liquid water is reduced in pressure within the regeneration container 108 through a nozzle. Below the saturation pressure, some of the liquid evaporates and rapidly expands. The mixture of vapor and liquid water is still mostly liquid on a mass basis, but mostly vapor on a volume basis. The rapid expansion generates a high-temperature mist 614, and it is desirable that droplets of liquid water 608 are carried by the vapor into the surface of the sorbent structure 104 and through it. The vapor / liquid ratio can be controlled to some extent by the supply temperature and pressure. Optionally, some embodiments may also provide auxiliary steam. In some embodiments, a second liquid pump 606, in fluid communication with the liquid water supply device, can pressurize the heated liquid water delivered to the nozzle 610 in the regeneration container 108.

[0094]

[0099] According to various embodiments, the system 600 may include a direct condenser 618 that extracts heat and condenses steam through direct contact with cooling water 614, rather than through indirect heat exchange as seen in some of the other embodiments described. The use of cooling water 614 may be extended to one or more compressors 126. In some embodiments, the steam mixture 132 after the condenser may be compressed by one or more liquid-sealed compressors that use water, in this case a portion of the cooling water 614, to form an internal seal. This provides direct cooling, which is further enhanced by the use of chilled water. In other embodiments, other types of vacuum compressors may be used.

[0095]

[0100] The removed water is then heated and recirculated to the liquid water supply device 110 along with makeup water 612 to compensate for some of the unavoidable water loss during the operation of the system 600. Optionally, according to some embodiments, a heat pump cycle can be used to simultaneously generate both refrigeration for condensation and heat for reheating.

[0096]

[0101] As with many other embodiments, part of the purification process of this system 600 involves separating the sorbate gas and volatile gas from water vapor through an aqueous phase transition. First, the water vapor condenses into a liquid, while the remainder remains in gaseous form. Next, the remaining water vapor is frozen into solid water and separated. Finally, the sorbate gas is liquefied and pressurized for later use.

[0097]

[0102] The freezing of water is a batch step that operates in a switching cycle. It is desirable to recover the water for reuse by melting the ice formed in this step. According to various embodiments, the system 600 may utilize two or more switching heat exchangers 624a and 624b that can operate between 0°C and -50°C. One heat exchanger (e.g., exchanger 624a) is used, and as the purified gas is separated from the ice, the frozen residual water accumulates over time. When the ice reaches a predefined level, or after a certain amount of time, or based on other metrics, the position of the exchanger is switched. The other exchanger 624b is used and becomes the recipient of the subsequent first sorbent product gas 140 from the front-end subsystem. The first exchanger 624a is now filled with ice and is reconfigured to remove the water. For example, using heat from the heat pump 120 and / or ambient heat and / or an external heat source, the frozen water is melted, and the resulting liquid water is sent along with the remaining recovered water. According to various embodiments, two or more switches continuously switch roles, each functioning to improve the efficiency and effectiveness of system 600.

[0098]

[0103] As shown, in some embodiments, the system 600 may utilize a distillation unit 602 to provide multiple condensation steps, thereby achieving better separation of the sorbent 102 (e.g., carbon dioxide) from volatile atmospheric gases. Exemplary distillation units include, but are not limited to, partial condensers or drip membrane condensers. Such a distillation unit 602 can be a simple instrument component for performing distillation. Note that if the sorbent 102 is carbon dioxide 103, this distillation must be performed at a temperature above 520 kPa to avoid the formation of carbon dioxide solids.

[0099]

[0104] In some embodiments, the distillation unit 602 may include a rectification section for reducing the concentration of carbon dioxide 103 in the distillate vapor and / or a stripping section for reducing the concentration of highly volatile components in the bottom liquid. According to various embodiments, the distillation unit 602 is in thermal contact with a second heat pump (i.e., a back-end heat pump).

[0100]

[0105] Next, the high-purity liquid carbon dioxide from the distillation unit 602 can be pumped up to high pressure using one or more high-density fluid pumps. In this way, carbon dioxide can be supplied at supercritical pressure, which is preferable for pipeline transfer for geological sequestration or to facilitate oil recovery.

[0101]

[0106] If the above examples, embodiments, and implementations are for reference only, those skilled in the art should understand that other systems and methods for efficiently capturing sorbent gases can be mixed with or substituted for the systems and methods provided. Where the above description refers to specific embodiments of systems and methods for efficiently capturing sorbent gases, it is readily apparent that many modifications can be made without departing from the spirit thereof, and that these embodiments and implementations can similarly be applied to other gas recovery technologies. Accordingly, the disclosed subject matter is intended to encompass the spirit and scope of this disclosure, as well as all changes, modifications, and variations that are in the knowledge of those skilled in the art. [Form 1] A recycled container comprising an opening and configured to enclose an sorbent structure physically moved through the opening, wherein the sorbent structure comprises the sorbent material on which the sorbent gas is sorbed, A liquid water supply device is connected to the aforementioned regeneration container so as to be able to communicate with it and is heated to a first temperature to generate steam, At least one heat pump, each of the at least one heat pumps includes at least one closed fluid circuit, at least one heat pump condenser, at least one heat pump evaporator, at least one heat pump pressure reducer, at least one refrigerant, and at least one heat pump compressor, and each closed fluid circuit includes one of the at least one heat pump condensers, one of the at least one heat pump evaporators, one of the at least one refrigerant, one of the at least one heat pump pressure reducers, and one of the at least one heat pump compressor, A condenser connected to the regeneration container and also connected to the liquid water supply device via a liquid pump, wherein the condenser is in thermal contact with a first closed fluid circuit of at least one heat pump, the first closed fluid circuit is also in thermal contact with the liquid water supply device, and as a result, heat is removed from the condenser at a second temperature lower than the first temperature, and heat is supplied to the liquid water supply device at the first temperature by the first closed fluid circuit. A first compressor connected to the condenser so as to be able to communicate with the condenser and Includes, The adsorbent structure in the regeneration container is such that, after the regeneration container is evacuated to a total pressure lower than the pressure corresponding to the saturated vapor pressure of water at a first temperature, it comes into fluid contact with the water vapor from the liquid water supply device at the first temperature, and when the water vapor comes into contact with the adsorbent material, a portion of the adsorbent gas is released, a vapor mixture containing the adsorbent gas and the water vapor is formed, and the total pressure is raised higher than the triple point pressure of the adsorbent. The steam mixture is removed from the regeneration container, cooled by the condenser, a portion of the steam in the steam mixture is condensed into liquid water, and returned to the liquid water supply device by the liquid pump. The remainder of the vapor mixture is compressed by the first compressor into a first sorbent product gas. The aforementioned sorbed material gas contains carbon dioxide. The at least one heat pump further includes a second closed fluid circuit and a third closed fluid circuit, The first sorbent product gas is in thermal contact with the heat pump evaporator of the second closed fluid circuit of the at least one heat pump. The second closed fluid circuit extracts heat from the first sorbate product gas at a third temperature lower than the second temperature and lower than the melting point of water, thereby obtaining the second sorbate product gas and solid water at the third temperature. The heat extracted by the second closed fluid circuit is supplied by the second closed fluid circuit to the liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second temperature and the first temperature. The second sorbent product gas is in thermal contact with the heat pump evaporator of the third closed fluid circuit of the at least one heat pump. The third closed fluid circuit extracts heat from the second sorbate product gas at a fifth temperature lower than the third temperature and lower than the boiling point of the sorbate, thereby obtaining a liquefied sorbate and a volatile gas at the fifth temperature. A system for recovering sorbent gas from sorbent material. [Form 2] The first closed fluid circuit and the second closed fluid circuit belong to the same heat pump. The system described in Form 1. [Form 3] The first closed fluid circuit, the second closed fluid circuit, and the third closed fluid circuit belong to the same heat pump. The system described in Form 1. [Form 4] The aforementioned sorbent material is solid. The system described in Form 1. [Form 5] The aforementioned sorbent material includes at least one of the following: an ion exchange resin, a functionalized polymer, activated carbon, a carbonate, a phosphate, a material containing an amine group, a material containing an ammonium group, and a material containing both an amine group and an ammonium group. The system described in Form 4. [Form 6] The adsorbent gas is removed from the adsorbent by at least one of temperature swing, pressure swing, and moisture swing. The system described in Form 1. [Form 7] The first temperature is between 40°C and 120°C. The system described in Form 1. [Form 8] The second temperature is between 0°C and 40°C. The system described in Form 1. [Form 9] The third temperature is between 0°C and -56°C. The system described in Form 1. [Form 10] At least a portion of the solid water is melted and transferred to the liquid water supply device. The system described in Form 1. [Form 11] The solid water is melted using ambient heat. The system described in Form 10. [Form 12] The solid water is melted using heat supplied by one of the at least one heat pumps. The system described in Form 10. [Form 13] The volatile gas comprises at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The system described in Form 1. [Form 14] The third temperature is selected to be sufficiently low such that the concentration of water in the second sorbate product gas at the third temperature is lower than the water solubility concentration of the liquefied sorbate at the fifth temperature. The system described in Form 1. [Form 15] The mechanical pump further includes a pump configured to receive the liquefied sorbent and to further increase the pressure of the liquefied sorbent, The system described in Form 1. [Form 16] The final pressure of the liquefied sorbate is at least equal to the supercritical pressure of carbon dioxide. The system described in Form 1. [Form 17] Before the water condensed as liquid water at the second temperature by the condenser is returned to the liquid water supply device, it is first heated by ambient heat to a sixth temperature close to or below the ambient temperature. The system described in Form 1. [Form 18] The first temperature rises during heating such that the temperature difference between the water vapor and the sorbent structure is minimized. The system described in Form 1. [Form 19] A regenerative container configured to enclose an sorbent structure containing an sorbent material on which an sorbent gas has been sorbed, A liquid water supply device is connected to the aforementioned regeneration container so as to be able to communicate with it and is heated to a first temperature to generate steam, At least one heat pump, A condenser that is connected to the regeneration container and also connected to the liquid water supply device via a liquid pump, the condenser being in thermal contact with a first heat pump of at least one heat pump, the heat pump also being in thermal contact with the liquid water supply device, and as a result, heat is removed from the condenser at a second temperature lower than the first temperature and supplied to the liquid water supply device by the first heat pump at the first temperature, A first compressor connected to the condenser so as to be able to communicate with the condenser and Includes, The adsorbent structure in the regeneration container is subjected to fluid contact with water vapor from the liquid water supply device at the first temperature after the regeneration container has been evacuated to a total pressure lower than the pressure corresponding to the saturated vapor pressure of water at the first temperature, the water vapor comes into contact with the adsorbent material, releasing a portion of the adsorbent gas to form a vapor mixture containing the adsorbent gas and water vapor, and raising the total pressure to a level higher than the triple point pressure of the adsorbent. The steam mixture is removed from the regeneration container, cooled by the condenser, a portion of the steam in the steam mixture is condensed into liquid water, and returned to the liquid water supply device by the liquid pump. The remainder of the steam mixture is compressed by the first compressor into a first sorbent product gas. A system for recovering sorbent gas from sorbent material. [Form 20] The first sorbed product gas is in thermal contact with the second heat pump of the at least one heat pump. The second heat pump extracts heat from the first sorbate product gas at a third temperature that is lower than the second temperature and lower than the melting point of water, thereby obtaining the second sorbate product gas and solid water at the third temperature. The system described in Form 19. [Form 21] The heat extracted by the second heat pump of at least one of the heat pumps is supplied by the second pump to the liquid water supply device at the first temperature and to the first heat pump at a fourth temperature between the second temperature and the first temperature. The system described in Form 20. [Form 22] The second sorbed product gas is in thermal contact with the third heat pump of at least one of the heat pumps. The third heat pump extracts heat from the second sorbate product gas at a fifth temperature that is lower than the third temperature and lower than the boiling point of the sorbate, thereby obtaining a liquefied sorbate and a volatile gas at the fifth temperature. The system described in form 20 or 21. [Form 23] The first heat pump and the second heat pump are the same heat pump. The system described in form 20 or 21. [Form 24] The first heat pump, the second heat pump, and the third heat pump are all the same heat pump. The system described in form 22. [Form 25] The regeneration container includes an opening through which the sorbent structure physically moves when transitioning between capturing the sorbent and releasing the sorbent for recovery. A system described in any one of Forms 19 to 24. [Form 26] The sorbed substance contains carbon dioxide. A system described in any one of Forms 19 to 25. [Form 27] The at least one heat pump operates as one of the following: a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator. The system described in Form 19. [Form 28] Each of the at least one heat pumps is: At least one closed fluid circuit, At least one heat pump condenser, At least one heat pump evaporator, At least one heat pump pressure reducer, At least one refrigerant, At least one heat pump compressor and Includes, Each closed fluid circuit includes one of the at least one heat pump condensers, one of the at least one heat pump evaporators, one of the at least one refrigerant, one of the at least one heat pump pressure reducer, and one of the at least one heat pump compressor. The system described in Form 19. [Form 29] The first sorbent product gas is in thermal contact with the heat pump evaporator of the second closed fluid circuit of the at least one heat pump. The second closed fluid circuit extracts heat from the first sorbate product gas at a third temperature lower than the second temperature and lower than the melting point of water, thereby obtaining the second sorbate product gas and solid water at the third temperature. The system described in Form 28. [Form 30] The heat extracted by the second closed fluid circuit is supplied by the second closed fluid circuit to the liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second temperature and the first temperature. The system described in Form 29. [Form 31] The second sorbed product gas is in thermal contact with the heat pump evaporator of the third closed fluid circuit of the at least one heat pump. The third closed fluid circuit extracts heat from the second sorbate product gas at a fifth temperature lower than the third temperature and lower than the boiling point of the sorbate, thereby obtaining a liquefied sorbate and a volatile gas at the fifth temperature. The system described in form 29 or 30. [Form 32] The first closed fluid circuit and the second closed fluid circuit belong to the same heat pump. The system described in form 29 or 30. [Form 33] The first closed fluid circuit, the second closed fluid circuit, and the third closed fluid circuit belong to the same heat pump. The system described in form 31. [Form 34] The aforementioned sorbent material is solid. The system described in Form 19. [Form 35] The aforementioned sorbent material includes at least one of an ion exchange resin, a functionalized polymer, activated carbon, a carbonate, a phosphate, a material containing an amine group, a material containing an ammonium group, and a material containing both an amine group and an ammonium group. The system described in Form 34. [Form 36] The adsorbent is removed from the adsorbent by at least one of the temperature swing, pressure swing, and moisture swing. The system described in Form 19. [Form 37] The first temperature is between 40°C and 120°C. The system described in any one of forms 19, 21, and 30. [Form 38] The second temperature is between 0°C and 40°C. The system described in any one of forms 19, 21, and 30. [Form 39] The third temperature is between 0°C and -56°C. The system described in form 20 or 31. [Form 40] At least a portion of the solid water is melted and transferred to the liquid water supply device. The system described in form 20 or 31. [Form 41] The solid water is melted using ambient heat. The system described in Form 40. [Form 42] The solid water is melted using heat supplied by one of the at least one heat pumps. The system described in Form 40. [Form 43] The volatile gas comprises at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The system described in form 22 or 31. [Form 44] The fluid contains a highly volatile component in an amount of 10 mol% or less. The system described in form 22 or 31. [Form 45] The pressure inside the regeneration container while the adsorbent structure is exposed to the water vapor is between 520 kPa and 3000 kPa. The system described in Form 19. [Form 46] The third temperature is selected to be sufficiently low such that the concentration of water in the second sorbate product gas at the third temperature is lower than the water solubility concentration in the liquefied sorbate at the fifth temperature. The system described in form 22 or 31. [Form 47] The mechanical pump further includes a pump configured to receive the liquefied sorbent and to further increase the pressure of the liquefied sorbent. The system described in form 22 or 31. [Form 48] The final pressure of the liquefied sorbate is at least equal to the supercritical pressure of carbon dioxide. The system described in Form 47. [Form 49] The water condensed as liquid water at the second temperature by the condenser is first heated by ambient heat to a sixth temperature close to or lower than the ambient temperature before being returned to the liquid water supply device. The system described in Form 19. [Form 50] The steam supplied to the regeneration container increases the total pressure of the regeneration container and maintains it at a pressure corresponding to or near the saturated vapor pressure. The system described in Form 19. [Form 51] The recycling container is maintained at a total pressure that is at least 85% of the saturation pressure of water at the first temperature. The system described in Form 50. [Form 52] The fluid connection between the liquid water supply device at the first temperature and the regeneration container is intermittently closed so that the total pressure of the released sorbed material gas exceeds the saturated vapor pressure of water vapor at the first temperature. The system described in Form 19. [Form 53] A portion of the water vapor that comes into contact with the adsorbent material transfers heat to the adsorbent material through at least one of sensible heat transfer, condensation, absorption, adsorption, and exothermic reactions. The system described in Form 19. [Form 54] A portion of the water vapor combines with the sorbent gas, and as a result, the total pressure of the regeneration container becomes higher than the vapor pressure of the sorbent vapor in equilibrium with the sorbent material. The system described in Form 19. [Form 55] The first temperature rises during heating such that the temperature difference between the water vapor and the sorbent structure is minimized. The system described in Form 19. [Form 56] The regeneration container further includes at least one nozzle located within the regeneration container and connected to the liquid water supply device in a manner that allows communication with the liquid water supply device, The heated liquid water from the liquid water supply device passes through the at least one nozzle, and when a portion of the heated liquid water expands into steam, the steam is introduced into the regeneration container, generating a hot mist containing the steam and water droplets. The system described in Form 19. [Form 57] The system further includes a second liquid pump that is in fluid communication with the liquid water supply device and pressurizes the heated liquid water that is sent to the at least one nozzle in the regeneration container, The system described in form 56. [Form 58] The second sorbate product gas is condensed in a distillation unit that is thermally in contact with the second heat pump of at least one heat pump. The distillation unit condenses the second sorbate product gas into a liquefied sorbate and a volatile gas. The system described in form 20 or 21. [Form 59] The second sorbate product gas is condensed in a distillation unit that is thermally in contact with the heat pump evaporator of the second closed fluid circuit of the at least one heat pump. The distillation unit condenses the second sorbate product gas into a liquefied sorbate and a volatile gas. The system described in form 29 or 30. [Form 60] The system further includes a fourth heat pump among the at least one heat pumps mentioned above. The fourth heat pump and the second heat pump are in intermittent fluid contact with the first adsorbent product gas, and as a result, when one of the fourth heat pump and the second heat pump is in fluid contact with the first adsorbent product gas, the other of the fourth heat pump and the second heat pump is isolated from the first adsorbent product gas. The fourth heat pump extracts heat from the first sorbate product gas at the third temperature, thereby obtaining the second sorbate product gas and solid water at the third temperature. The system is configured such that when one of the fourth heat pump and the second heat pump is in fluid contact with the first adsorbed material product gas, at least a portion of the solid water that is in thermal contact with the other of the fourth heat pump and the second heat pump melts and is transferred to the liquid water supply device. The system described in Form 20. [Form 61] The system further includes a fourth closed fluid circuit of at least one of the heat pumps, The fourth closed fluid circuit and the second closed fluid circuit are in intermittent fluid contact with the first sorbate product gas, and as a result, when one of the fourth closed fluid circuit and the second closed fluid circuit is in fluid contact with the first sorbate product gas, the other of the fourth closed fluid circuit and the second closed fluid circuit is isolated from the first sorbate product gas. The fourth closed fluid circuit extracts heat from the first sorbate product gas at the third temperature, and as a result, a second sorbate product gas and solid water are obtained at the third temperature. The system is configured such that when one of the fourth closed fluid circuit and the second closed fluid circuit is in fluid contact with the first adsorbent product gas, at least a portion of the solid water that is in thermal contact with the other of the fourth closed fluid circuit and the second closed fluid circuit melts and is transferred to the liquid water supply device. The system described in Form 29. [Form 62] A step of housing an sorbent structure in a regenerating container, wherein the sorbent structure includes the sorbent material on which the sorbent gas has been sorbed, A step of generating steam by supplying heat at a first temperature to a liquid water supply device, The steps include reducing the total pressure of the recycling container to a pressure less than the pressure corresponding to the saturated vapor pressure of water at the first temperature, The steps include: introducing the steam at the first temperature into the regeneration container, bringing the steam into fluid contact with the sorbent material, releasing a portion of the sorbent gas to form a steam mixture containing the sorbent gas and the steam, and raising the total pressure in the regeneration container to a level higher than the triple point pressure of the sorbent; A step that enables the steam mixture to flow out of the regeneration container by bringing the steam mixture into fluid contact with a condenser that is connected to the regeneration container and also connected to the liquid water supply device via a liquid pump, wherein the condenser is in thermal contact with a first heat pump that is also in thermal contact with the liquid water supply device, and the first heat pump is one of at least one heat pumps, The steps include using the first heat pump to remove heat from the steam mixture at a second temperature lower than the first temperature, and condensing a portion of the water vapor in the steam mixture into liquid water, The steps include providing the heat removed from the steam mixture at the second temperature to the liquid water supply device at the first temperature, The steps include: using the liquid pump to return the liquid water condensed from the steam mixture to the liquid water supply device; The steps include compressing the remainder of the vapor mixture in a first compressor connected to the condenser so as to communicate with it, thereby forming a first sorbent product gas, and including, A method for recovering sorbent gas from sorbent material. [Form 63] The method further includes a step of extracting heat from the first sorbent product gas at a third temperature using a second heat pump that is in thermal contact with the first sorbent product gas, thereby obtaining a second sorbent product gas and solid water at the third temperature. The third temperature is lower than the second temperature and also lower than the melting point of water. The method described in form 62. [Form 64] The further step includes providing the heat extracted by the second heat pump of the at least one heat pump to one of the liquid water supply device at a first temperature and the first heat pump at a fourth temperature between the second and first temperatures. The method described in form 63. [Form 65] The process includes a step of extracting heat from the second sorbate product gas at a fifth temperature using a third heat pump that is in thermal contact with the second sorbate product gas, thereby obtaining a liquefied sorbate and a volatile gas at the fifth temperature. The fifth temperature is lower than the third temperature and also lower than the boiling point of the sorbed material. The method according to form 63 or 64. [Form 66] The first heat pump and the second heat pump are the same heat pump. The method according to form 63 or 64. [Form 67] The first heat pump, the second heat pump, and the third heat pump are the same heat pump. The method described in form 65. [Form 68] The further step includes physically moving the sorbent structure into the regeneration container through the opening of the regeneration container before reducing the total pressure of the regeneration container, The method described in any one of forms 62 to 67. [Form 69] The sorbed substance contains carbon dioxide. The method described in any one of forms 62 to 68. [Form 70] The at least one heat pump operates as one of the following: a vapor compression cycle, a vapor absorption cycle, a vapor adsorption cycle, or a thermoelectric refrigerator. The method described in form 62. [Form 71] Each of the at least one heat pumps is: At least one closed fluid circuit, At least one heat pump condenser, At least one heat pump evaporator, At least one heat pump pressure reducer, At least one refrigerant, At least one heat pump compressor and Includes, Each closed fluid circuit includes one of the at least one heat pump condensers, one of the at least one heat pump evaporators, one of the at least one refrigerant, one of the at least one heat pump pressure reducer, and one of the at least one heat pump compressor. The method described in form 62. [Form 72] The method further includes a step of extracting heat from the first sorbent product gas at a third temperature using a second closed fluid circuit of at least one heat pump that is in thermal contact with the first sorbent product gas, thereby obtaining a second sorbent product gas and solid water at the third temperature. The third temperature is lower than the second temperature and also lower than the melting point of water. The method described in form 71. [Form 73] The further step includes providing the heat extracted by the second closed fluid circuit to the liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second temperature and the first temperature. The method described in form 72. [Form 74] The process includes a step of extracting heat from the second sorbent product gas at a fifth temperature using a third closed fluid circuit of at least one heat pump that is in thermal contact with the second sorbent product gas, thereby obtaining a liquefied sorbent and a volatile gas at the fifth temperature. The fifth temperature is lower than the third temperature and also lower than the boiling point of the sorbed material. The method according to embodiment 72 or 73. [Form 75] The first closed fluid circuit and the second closed fluid circuit belong to the same heat pump among the at least one heat pump. The method according to embodiment 72 or 73. [Form 76] The first closed fluid circuit, the second closed fluid circuit, and the third closed fluid circuit belong to the same heat pump among the at least one heat pump. The method described in form 74. [Form 77] The aforementioned sorbent material is solid. The method described in form 62. [Form 78] The aforementioned sorbent material includes at least one of the following: an ion exchange resin, a functionalized polymer, activated carbon, a carbonate, a phosphate, a material containing an amine group, a material containing an ammonium group, and a material containing both an amine group and an ammonium group. The method described in form 77. [Form 79] The adsorbent is removed from the adsorbent by at least one of the temperature swing, pressure swing, and moisture swing. The method described in form 62. [Form 80] The first temperature is between 40°C and 120°C. The method according to any one of embodiments 62, 64, and 73. [Form 81] The second temperature is between 0°C and 40°C. The method according to any one of embodiments 62, 64, and 73. [Form 82] The third temperature is between 0°C and -56°C. The method according to form 63 or 74. [Form 83] The further step includes dissolving at least a portion of the solid water and adding the water to the liquid water supply device. The method according to form 63 or 74. [Form 84] The solid water is melted using ambient heat. The method described in form 83. [Form 85] The solid water is melted using the heat provided by one of the at least one heat pumps. The method described in form 83. [Form 86] The volatile gas comprises at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The method according to form 65 or 74. [Form 87] The fluid contains a highly volatile component in an amount of 10 mol% or less. The method according to form 65 or 74. [Form 88] The pressure inside the regeneration container while the adsorbent structure is exposed to the water vapor is between 520 kPa and 3000 kPa. The method described in form 62. [Form 89] The third temperature is selected to be sufficiently low such that the concentration of water in the second sorbate product gas at the third temperature is lower than the water solubility concentration in the liquefied sorbate at the fifth temperature. The method according to form 65 or 74. [Form 90] The further step includes increasing the pressure of the liquefied sorbent using a mechanical pump configured to receive the liquefied sorbent, The method according to form 65 or 74. [Form 91] The final pressure of the liquefied sorbate is at least equal to the supercritical pressure of carbon dioxide. The method described in form 90. [Form 92] The further step includes, before returning the liquid water to the liquid water supply device, using ambient heat to heat the liquid water condensed from the vapor mixture to a sixth temperature near or below the ambient temperature. The method described in form 62. [Form 93] The steam supplied to the regeneration container increases the total pressure of the regeneration container and maintains it at a pressure corresponding to or near the saturated vapor pressure. The method described in form 62. [Form 94] The recycling container is maintained at a total pressure that is at least 85% of the saturation pressure of water at the first temperature. The method described in form 93. [Form 95] The further step includes intermittently closing the fluid connection between the liquid water supply device at the first temperature and the regeneration container, The released sorbate gas causes the total pressure in the regeneration container to rise to a level exceeding the saturated vapor pressure of water vapor at the first temperature. The method described in form 62. [Form 96] A portion of the water vapor that comes into contact with the adsorbent material transfers heat to the adsorbent material through at least one of sensible heat transfer, condensation, absorption, adsorption, and exothermic reactions. The method described in form 62. [Form 97] A portion of the water vapor combines with the sorbent gas, and as a result, the total pressure of the regeneration container becomes higher than the vapor pressure of the sorbent vapor in equilibrium with the sorbent material. The method described in form 62. [Form 98] The first temperature rises during heating such that the temperature difference between the water vapor and the sorbent structure is minimized. The method described in form 62. [Form 99] The step further includes using the volatile gas as a heat sink at the fifth temperature, The method according to form 65 or 74. [Form 100] The step further includes using the volatile gas at the fifth temperature to produce a useful effect, The method according to form 65 or 74. [Form 101] The process further includes using the volatile gas at the fifth temperature as a source of drying gas as part of the drying process. The method according to form 65 or 74. [Form 102] The step further includes using the volatile gas at the fifth temperature as a source of dry gas for the operation of the pneumatic device, The method according to form 65 or 74. [Form 103] The generation of the steam includes the step of passing heated liquid water from the liquid water supply device through at least one nozzle, The nozzle is located inside the regeneration container and is connected to the liquid water supply device so as to be able to communicate with it. A portion of the heated liquid water expands to become steam, generating a hot mist containing the steam and water droplets within the regeneration container. The method described in form 62. [Form 104] The step further includes pressurizing the heated liquid water to be sent to the at least one nozzle in the regeneration container using a second liquid pump that is in fluid communication with the liquid water supply device, The method described in morphology 103. [Form 105] The process further includes the step of condensing the second sorbate product gas in a distillation unit that is thermally in contact with the second heat pump, The distillation unit condenses the second sorbate product gas into a liquefied sorbate and a volatile gas. The method according to form 63 or 64. [Form 106] The step further includes condensing the second sorbent product gas in a distillation unit that is thermally in contact with the heat pump evaporator of the second closed fluid circuit of at least one heat pump, The distillation unit condenses the second sorbate product gas into a liquefied sorbate and a volatile gas. The method according to embodiment 72 or 73. [Form 107] A step of intermittently bringing the second heat pump and the fourth heat pump into fluid contact with the first sorbate product gas, wherein, as a result, when one of the fourth heat pump and the second heat pump is in fluid contact with the first sorbate product gas, the other of the fourth heat pump and the second heat pump is isolated from the first sorbate product gas. A step of extracting heat from the first sorbate product gas at the third temperature using the fourth heat pump, thereby obtaining a second sorbate product gas and solid water at the third temperature. The fourth heat pump and the other of the second heat pump, while in fluid contact with the first sorbate product gas, are in thermal contact with one of the fourth heat pump and the second heat pump to melt at least a portion of the solid water, The steps include transferring the liquid water from a portion of the molten solid water to the liquid water supply device, and The method according to embodiment 63, further comprising: [Form 108] A step of intermittently bringing the second heat pump and the fourth closed fluid circuit into fluid contact with the first sorbate product gas, wherein, as a result, when one of the fourth closed fluid circuit and the second closed fluid circuit is in fluid contact with the first sorbate product gas, the other of the fourth closed fluid circuit and the second closed fluid circuit is isolated from the first sorbate product gas. A step of extracting heat from the first sorbate product gas at the third temperature using the fourth closed fluid circuit, wherein a second sorbate product gas and solid water are obtained at the third temperature. The other of the fourth closed fluid circuit and the second closed fluid circuit melts at least a portion of the solid water that is in thermal contact with one of the fourth closed fluid circuit and the second closed fluid circuit while in fluid contact with the first sorbate product gas, The steps include transferring the liquid water from the aforementioned portion of the molten solid water to the liquid water supply device. The method according to embodiment 72, further comprising:

Claims

1. A system for recovering sorbent gas from an sorbent material, A recycled container comprising an opening and configured to enclose an sorbent structure physically moved through the opening, wherein the sorbent structure comprises the sorbent material on which the sorbent gas is sorbed, A liquid water supply device is connected to the aforementioned regeneration container so as to be able to communicate with it and is heated to a first temperature to generate steam, At least one heat pump, each of the at least one heat pumps includes at least one closed fluid circuit, at least one heat pump condenser, at least one heat pump evaporator, at least one heat pump pressure reducer, at least one refrigerant, and at least one heat pump compressor, and each closed fluid circuit includes one of the at least one heat pump condensers, one of the at least one heat pump evaporators, one of the at least one refrigerant, one of the at least one heat pump pressure reducers, and one of the at least one heat pump compressor, A condenser connected to the regeneration container and also connected to the liquid water supply device via a liquid pump, wherein the condenser is in thermal contact with a first closed fluid circuit of at least one heat pump, and the first closed fluid circuit is also in thermal contact with the liquid water supply device, so that heat is removed from the condenser at a second temperature lower than the first temperature, and heat is supplied to the liquid water supply device at the first temperature by the first closed fluid circuit, A first compressor connected to the condenser so as to be able to communicate with the condenser and Includes, The adsorbent structure in the regeneration container is such that, after the regeneration container is evacuated to a total pressure lower than the pressure corresponding to the saturated vapor pressure of water at a first temperature, it comes into fluid contact with the water vapor from the liquid water supply device at the first temperature, and when the water vapor comes into contact with the adsorbent material, a portion of the adsorbent gas is released, a vapor mixture containing the adsorbent gas and the water vapor is formed, and the total pressure is raised to a level higher than the triple point pressure of the adsorbent. The steam mixture is removed from the regeneration container, cooled by the condenser, a portion of the steam in the steam mixture is condensed into liquid water, and returned to the liquid water supply device by the liquid pump. The remainder of the steam mixture is compressed by the first compressor into a first sorbent product gas. The aforementioned sorbed material gas contains carbon dioxide. The at least one heat pump further includes a second closed fluid circuit and a third closed fluid circuit, The first sorbed product gas is in thermal contact with the heat pump evaporator of the second closed fluid circuit of the at least one heat pump. The second closed fluid circuit extracts heat from the first sorbate product gas at a third temperature lower than the second temperature and lower than the melting point of water, and as a result, the second sorbate product gas and solid water are obtained at the third temperature. The heat extracted by the second closed fluid circuit is supplied by the second closed fluid circuit to the liquid water supply device at the first temperature and to one of the first closed fluid circuits downstream of the heat pump evaporator of the first closed fluid circuit at a fourth temperature between the second temperature and the first temperature. The second sorbed product gas is in thermal contact with the heat pump evaporator of the third closed fluid circuit of the at least one heat pump. The third closed fluid circuit extracts heat from the second sorbate product gas at a fifth temperature lower than the third temperature and lower than the boiling point of the sorbate, thereby obtaining a liquefied sorbate and a volatile gas at the fifth temperature. system.

2. The first closed fluid circuit and the second closed fluid circuit belong to the same heat pump. The system according to claim 1.

3. The first closed fluid circuit, the second closed fluid circuit, and the third closed fluid circuit belong to the same heat pump. The system according to claim 1.

4. The aforementioned sorbent material is solid. The system according to claim 1.

5. The aforementioned sorbent material includes at least one of the following: an ion exchange resin, a functionalized polymer, activated carbon, a carbonate, a phosphate, a material containing an amine group, a material containing an ammonium group, and a material containing both an amine group and an ammonium group. The system according to claim 4.

6. The adsorbent gas is removed from the adsorbent by at least one of temperature swing, pressure swing, and moisture swing. The system according to claim 1.

7. The first temperature is between 40°C and 120°C. The system according to claim 1.

8. The second temperature is between 0°C and 40°C. The system according to claim 1.

9. The third temperature is between 0°C and -56°C. The system according to claim 1.

10. At least a portion of the solid water is melted and transferred to the liquid water supply device. The system according to claim 1.

11. The solid water is melted using ambient heat. The system according to claim 10.

12. The solid water is melted using heat supplied by one of the at least one heat pumps. The system according to claim 10.

13. The volatile gas comprises at least one of nitrogen, oxygen, methane, hydrogen, and carbon monoxide. The system according to claim 1.

14. The third temperature is selected to be sufficiently low such that the concentration of water in the second sorbate product gas at the third temperature is lower than the water solubility concentration of the liquefied sorbate at the fifth temperature. The system according to claim 1.

15. The system further includes a mechanical pump configured to receive the liquefied sorbent and to further increase the pressure of the liquefied sorbent. The system according to claim 1.

16. The final pressure of the liquefied sorbate is at least equal to the supercritical pressure of carbon dioxide. The system according to claim 1.

17. Before the water condensed as liquid water at the second temperature by the condenser is returned to the liquid water supply device, it is first heated by ambient heat to a sixth temperature close to or below the ambient temperature. The system according to claim 1.

18. The first temperature rises during heating such that the temperature difference between the water vapor and the sorbent structure is minimized. The system according to claim 1.

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