WO2025229587A1

WO2025229587A1 - Sorptive gas separation with chemical heat pumps for producing steam

Info

Publication number: WO2025229587A1
Application number: PCT/IB2025/054562
Authority: WO
Inventors: Nicholas Stiles WILKINS; Gaurav Chachra; Joel Cizeron
Original assignee: Svante Technologies Inc
Current assignee: Svante Technologies Inc
Priority date: 2024-05-01
Filing date: 2025-04-30
Publication date: 2025-11-06
Anticipated expiration: 2026-11-01

Abstract

An integrated sorptive gas separator can have a sorptive separator for separating a first component from a multi-component feed gas stream and producing a second product stream enriched in the first component relative to the multi-component feed gas stream, and a chemical heat pump for accepting the second product stream and sorbing the first component on and/or in a heat pump sorbent for producing a regeneration stream used in the sorptive gas separator.

Description

SORPTIVE GAS SEPARATION WITH CHEMICAL HEAT PUMPS FOR PRODUCING STEAM

FIELD

The present technology generally relates to integrated sorptive gas separation processes and systems using a solid sorbent and steam for regeneration of solid sorbent, and more particularly, sorptive gas separation processes and systems having integrated chemical heat pumps for producing steam for regeneration of solid sorbents.

BACKGROUND

Carbon dioxide (CO2) capture from waste streams is an industrial and environmental challenge of great importance for the foreseeable future. Solutions to this challenge utilizing solid sorbents have significant scalability advantages over other methods but the cost of CO2 capture should be minimized to enable rapid adoption assisting the transition towards net zero greenhouse gas (GHG) emission in the medium-term future.

Moisture and temperature swing sorption methods are known in the art for use in the sorptive separation of multi-component gas mixtures. These methods are used for sorbing a target component of an influent, or feed stream of a sorptive separator, on and/or in a solid sorbent material, thereby separating the sorbed target component from the remaining components in the feed stream, and subsequently regenerating the sorbent, allowing for cyclic reuse of the sorbent.

In some methods, water in the form of steam, can be employed as a regeneration medium to desorb the sorbed target component from the sorbent, thereby regenerating the sorbent material. The sorbed water is removed in a subsequent conditioning step by admitting a stripping gas stream (also referred to herein as a conditioning gas stream) with a low partial pressure of water relative to a partial pressure of water on and/or in the sorbent at the end of the regeneration step to contact the solid sorbent or by applying a vacuum in the regeneration step. Sorptive gas separation processes and systems employing solid sorbents offer many advantages including, for example, a compact foot-print, and reduced energy consumption relative to gas separation processes employing liquid absorbents.

Separation of one or more gas components from a multi-component gas stream may be desirable, such as for the removal and/or sequestration of an acid gas component, for example, carbon dioxide (CO2), from a flue gas stream, ambient air, HVAC air, a bio-methane gas stream, a natural gas stream, or a hydrocarbon gas stream. Example applications include: combustion processes; combined cycle processes; combined heat and power processes, where an oxidant and a carbon- containing fuel are combusted to generate, for example, heat, a combustion gas stream (also known as a combustion flue gas stream or a flue gas stream) and mechanical power, such as through expansion of combustion gases or other means of converting heat into mechanical work; direct air capture processes; and cement production processes. Typically, after separation of the target component, it is desirable to form and provide a product gas stream with the highest purity which can be a challenge for gas separation technologies.

Chemical heat pumps have been proposed for a variety of applications including harvesting water from atmospheric air. One advantage of such heat pumps is the ability to use different working fluids other than the traditional fluoro-hydrocarbons, or light hydrocarbons such as propane. One other advantage can be a reduction in compression ratio for the working fluid in the heating or cooling or combined heating and cooling process.

High energy consumption and the associated cost to produce steam for regeneration of the solid sorbents is a shortcoming of commercial adaptation of rapid cycle sorptive gas separators and processes. Steam can be formed in several ways. One method involves combustion of a hydrocarbon fuel in an auxiliary boiler which undesirably produces deleterious gases, including CO2, in addition to the main commercial or industrial process. Another shortcoming of this method is the increased total amount of CO2 produced by the auxiliary boiler which also should be separated and captured. Another method involves recovering waste heat from a commercial or industrial process with a typical heat pump using a cryogenic fluid. Shortcomings of this method include the use of a cryogenic fluid which can be harmful or hazardous to the environment, such as agents that can deplete the earth’s ozone layer (fluorocarbons) or flammable materials (propane), especially at larger scales with larger systems, and the requirement to store and maintain the cryogenic fluid as a dedicated working fluid for the chemical heat pump.

The present invention aims to eliminate the shortcomings of high energy costs for sorptive separation, the generation of additional pollutant(s) associated with the sorption separation process or the use of cryogenic fluids in the sorption separation process.

SUMMARY

In a broad aspect, an integrated sorptive gas separation process for separating a first component from a multi-component gas stream can have the following steps:

(a) admitting a multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, further comprising the steps of:

(i) sorbing the first component on and/or the sorbent,

(ii) recovering a first product stream depleted in the first component relative to the feed stream,

(iii) admitting a regeneration stream comprising a second component into the sorptive separator,

(iv) desorbing the first component from the sorbent, and recovering a second product stream from the sorptive separator, wherein the second product stream is enriched in the first component relative to the feed stream;

(b) admitting at least a portion of the second product stream into a first circuit of a vessel of a chemical heat pump, wherein the first circuit of the vessel is at a first pressure prior to admitting the at least a portion of the second product stream, increasing the pressure of the first circuit of the vessel to a second pressure, sorbing the first component on and/or in a heat pump sorbent in the first circuit of the vessel thus producing heat;

(c) reducing the pressure of the first circuit of the vessel to equal to or less than the first pressure, desorbing the first component from the heat pump sorbent, forming a chemical heat pump product stream, and recovering the chemical heat pump product stream from the first circuit of the vessel, and

(d) transferring the heat produced in step (b) to an aqueous liquid stream comprising a second component in a second circuit of the vessel of the chemical heat pump and converting at least a fraction of the liquid stream into a vapor comprising the second component or steam, for forming at least a portion of the regeneration stream, wherein in step (c) the chemical heat pump product stream is at least periodically enriched in the first component relative to the second product stream.

In another broad aspect, an integrated sorptive gas separation process for separating a first component from a multi-component gas stream includes the following steps:

(a) admitting the multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, further comprising the steps of:

(i) sorbing the first component on and/or in the sorbent in the sorptive separator,

(iv) desorbing the first component from the sorbent in the sorptive separator,

(v) adsorbing the second component one and/or in the sorbent in the sorptive separator,

(vi) recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator,

(vii) admitting a conditioning stream into the sorptive separator wherein the conditioning stream has a partial pressure of the second component less than a partial pressure of the second component around the sorbent in the sorptive separator measured at the end of recovery of the second product stream,

(viii) desorbing the second component from the sorbent in the sorptive separator to form a third product stream enriched in the second component relative to the conditioning stream, and

(ix) recovering the third product stream from the sorptive separator;

(b) admitting at least a portion of the third product stream into a first circuit of a vessel of a chemical heat pump wherein the first circuit of the vessel is at a pressure equal to or less than a first pressure and a first temperature before admitting the portion of the third product stream, increasing the pressure of the first circuit of the vessel to equal or greater than a second pressure, sorbing the second component on and/or in a heat pump sorbent in the first circuit of the vessel, producing heat and increasing the temperature within the first circuit of the vessel to equal or greater than a second temperature;

(c) reducing the pressure of the first circuit of the vessel to equal or less than the first pressure thereby desorbing the second component from the heat pump sorbent in the first circuit of the vessel, producing a chemical heat pump product stream, recovering the chemical heat pump product stream from the first circuit of the vessel, and

(d) transferring the heat produced in step (b) to an aqueous liquid stream comprising a second component and converting at least a fraction the liquid stream into a vapor comprising the second component for forming at least a portion of the regeneration stream.

In another broad aspect, an integrated sorptive gas separation system for separating a first component from a multi-component gas stream comprises:

(a) a sorptive separator further comprising a sorbent, a feed port for admitting the multi-component gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream from the sorptive separator, a regeneration port for admitting a regeneration stream into the sorptive separator, a second product port for recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator, wherein the feed port and first product port, is fluidly connected and the regeneration port and the second product port is fluidly connected; and

(b) a chemical heat pump further comprising at least one vessel with a first circuit having a heat pump sorbent and a second circuit, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream, a liquid inlet port fluidly connected to the second circuit of the vessel for admitting an aqueous liquid stream or a water stream into the second circuit, and a fluid outlet port fluidly connected to the second circuit of the vessel for recovering the aqueous liquid stream or a steam stream from the second circuit.

(a) a sorptive separator further comprising a sorbent, a feed port for admitting the multi-component gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream, a regeneration port for admitting a regeneration stream into the sorptive separator, a second product port for recovering a second product stream enriched in the first component relative to the feed stream, a conditioning port for admitting a conditioning stream into the sorptive separator, and a third product port for recovering a third product stream from the sorptive separator, wherein the feed port and first product port is fluidly connected, the regeneration port and the second product port is fluidly connected, and the conditioning port and the third product port is fluidly connected; and

(b) a chemical heat pump comprising at least one vessel with a first circuit having a heat pump sorbent, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream, wherein the third product port is fluidly connected to the working fluid port. In yet another broad aspect, a vessel of a chemical heat pump comprises: a vessel; a heat pump sorbent; a first circuit; and a second circuit, wherein the heat pump sorbent is configured as a film, layer, or sheet, having a thickness in a range of 0.1 and 1 mm, and interposed between the first circuit and the second circuit, and having a surface area per volume in a range of 250m²/m³ and 2500 m²/m³, and having a heat capacity equal to or greater than 50% of a heat capacity of the vessel when the first circuit and second circuit are filled with a gas.

BRIEF DESCRIPTION OF THE DRAWINGS

Fig. 1 is a schematic diagram illustrating embodiments of an integrated sorptive gas separation system and processes of operating the integrated sorptive gas separation system;

Fig. 2a is a diagram of a vessel of a chemical heat pump;

Fig. 2b is a cross-sectional view of the vessel shown in Fig. 2a;

Fig. 3 is a schematic diagram illustrating embodiments of an integrated sorptive gas separation system and processes of operating the integrated sorptive gas separation system;

Fig. 4 is a schematic diagram illustrating embodiments of an integrated sorptive gas separation system and processes of operating the integrated sorptive gas separation system

Fig. 5 is a schematic diagram illustrating embodiments of an integrated sorptive gas separation system and processes of operating the integrated sorptive gas separation system;

Fig. 6a is a schematic diagram illustrating a chemical heat pump with a plurality of vessels and processes of the chemical heat pump;

Fig. 6b is a simulated plot of pressure and temperature versus time of a vessel during the process illustrated in Fig. 6a; and

Fig. 7 is a simulated plot of the concentration of the first component versus time admitted into and recovered from a vessel of a chemical heat pump. DETAILED DESCRIPTION

Definitions:

Sorbent: a material that absorbs and/or adsorbs a target component, the material can be an absorbent or an adsorbent.

Chemical heat pump: a device which utilizes a reversible exothermic or endothermic chemical reaction, a sorption process which cycles between at least a sorption step and a desorption step, or a solubilization process to change the temperature of a solid or liquid enabling the transfer of heat from a hot reservoir or fluid to a cold solid or fluid. A chemical heat pump can have a heat exchanger which is integrated into the chemical heat pump with a working fluid circuit and a heat exchange circuit which are fluidly separate from each other; the heat exchange circuit uses a heat exchange fluid for transferring heat from and to the chemical heat pump, and a working fluid circuit for producing the chemical reaction and heat. A sorption heat pump is a type of chemical heat pump utilizing the heat of sorption released during sorption of a component on and/or in a sorbent.

Conditioning stream: a gas stream admitted into a sorptive separator during a conditioning step which contacts a solid sorbent of the sorptive separator. The primary purpose of the conditioning stream is at least one of stripping and/or purging water from the sorbent and/or sorptive separator. The conditioning stream has a lower partial pressure of water relative to a partial pressure of water on and/or in the sorbent at the end of the regeneration step. The conditioning step occurs after a regenerating step during the sorptive gas separation process.

DCC: Direct Contact Cooler, a device for reducing the temperature of a gas by admitting into the DCC a liquid and a gas where a temperature of liquid is less than a temperature of the gas, directly contacting the liquid with the gas, and retrieving a cooled gas and a heated liquid from the DCC.

Heat pump: an apparatus for heating or cooling a first medium by transferring heat by mechanical means from or to a second medium.

HEX: Heat Exchanger, a device for transferring heat from a first medium or stream to a second medium or stream, for example, through a solid barrier which prevents mixing of the first and second streams, or through a solid heat accumulator. Typical HEXs can be configured as a plate heat exchanger with alternative flow channels arranged between parallel plates, or a tubular heat exchanger (for example, a shell and tube, or a tube in tube) where a first stream flows in one or more tubes while a second stream flows on the outside of the one or more tubes.

HVAC air: Heating, ventilation, and air from an air conditioner, air from a confined space that is circulated, for example, air in of an office building which can be circulated with a controlled temperature, moisture content and CO2 content. Typically, HVAC air has a higher CO2 concentration than outside air.

Disclosed herein is an integrated sorptive gas separation system and process integrating a sorptive separator using a sorptive separation process with a chemical heat pump (herein referred to as “CHP”) using a chemical heat pump process (herein referred to as a “CHP process”). The sorptive separator uses a solid sorbent while the sorptive separation process can employ at least one swing mechanism, including, for example, a temperature swing, a moisture swing, a partial pressure swing, and a pressure swing. The CHP can use a solid sorbent while the CHP process can employ a swing mechanism, for example, pressure swing, to generate heat which can be used for producing a regeneration stream for the sorptive separator. The integrated sorptive gas separation system and process can be used for separating a target or a first component from a multi-component gas stream, for example, a flue gas stream, ambient air or HVAC air, a bio-methane gas stream, a natural gas stream, a hydrocarbon gas stream, or a gas stream having H2, CO, and CO2. The first component can be an acid gas component such as carbon dioxide (CO2) or a C2⁺ hydrocarbon.

A sorptive separator and sorptive separation process can be used for separating a target or a first component from a multi-component gas stream. The sorptive separation process comprises a sorbing step followed by a desorbing step (also referred to as “a regenerating step”). During the sorbing step, a multi-component gas stream comprising a target or a first component can be admitted as a feed stream into the sorptive separator to come in contact with a sorbent in the sorptive separator. As the feed stream contacts the sorbent, the first component can sorb in and/or on the sorbent, separating the first component from the feed stream and producing a first product stream depleted in the first component relative to the feed stream. The first product stream can then be recovered from the sorptive separator. During the regenerating step, a regeneration stream comprising a second component, for example, water (H2O) in the form of steam can be admitted into the sorptive separator to desorb the first component from the sorbent to produce a second product stream enriched in the first component relative to the feed stream. The second product stream can then be recovered from the sorptive separator.

A second product stream can comprise both the first component and a second component. In embodiments, it is desirable for the second component to be easily separated from the first component, have a boiling point above ambient temperature, and have a strong interaction or high selectivity with the sorbent. The energy for vaporization of the second component is one of the principal energy costs of the sorptive separation process using a partial pressure swing process.

In embodiments, a conditioning step can be used after a regenerating step where a stripping or a conditioning stream comprising a third component, for example, nitrogen (N2), or a gas stream with a low partial pressure of the second component, can be admitted into the sorptive separator to remove the second component from the sorbent, producing a third product stream. The third product stream can then be recovered from the sorptive separator.

A CHP and CHP process can be used for producing a regeneration stream for a sorptive separation process, such as assisting in converting a fluid stream comprising the second component from a liquid phase to a gas phase. The CHP comprises a sorbent and employs one of a working fluid comprising a first component (such as CO2 or a C2⁺ hydrocarbon), a second component (such as steam), or a fourth component (such as any suitable component other than CO2, H2O, or N2, in a gaseous phase). The working fluid can be sorbed and desorbed from the sorbent by a pressure swing mechanism which produces a heat of adsorption which can be recovered and used to assist in producing the regeneration stream for the sorptive separator. Additional heat can be recovered from a waste stream, an effluent stream, or cooling of one or more process streams within the integrated sorptive gas system and process to assist in producing the regeneration stream. The recovered heat can be used to increase the exergy of at least one low exergy fluid stream at a first temperature, to a higher exergy and a second temperature where the second temperature is greater than the first temperature.

In embodiments, the additional heat can be recovered from one or more streams of the integrated sorptive gas separation system and process such as, a feed stream prior to admitting into a sorptive separator, an interstage cooling stream of a compressor for compressing the second product stream recovered from the sorptive separator, and a conditioning effluent stream or third product stream recovered from the sorptive separator. As heat is recovered from one or more of these streams, its temperature can be reduced and water can be removed.

In an embodiment, a CHP can comprise a vessel with a solid sorbent, which can be configured to be on and/or in sorbent contactors or sorbent beds. In another embodiment, a CHP can comprise a plurality of vessels and during a CHP process, each vessel can be alternatively exposed to a working fluid in the gas phase using a pressure swing mechanism, cycling between: (1 ) a high pressure, or a high partial pressure of a first or a second component of the working fluid, and (2) a low pressure or a low partial pressure of the first or the second component of the working fluid. In an embodiment, a pressure ratio between the high partial pressure and the low partial pressure is at least 2:1 respectively when the working fluid is the first component or CO2.

In an embodiment, an integrated sorptive gas separation process and system can use the first component or CO2 separated and recovered from a second product stream of the sorptive separation process as the working fluid in a CHP and CHP process. Advantages include: no inventory of the working fluid is required for the chemical heat pump, and the second product stream from the sorptive separator can be further purified with the chemical heat pump increasing the purity of a product stream comprising the first component recovered from the integrated sorptive gas separation system thereby adding a second functionality for the chemical heat pump.

For example, a sorptive separator can produce a second product stream with a concentration of 90% by volume of the first component or CO2, which can be directed to the chemical heat pump to produce a chemical heat pump product stream with a concentration of 98% by volume of the first component or CO2. If the first component or CO2 is used as a working fluid in a CHP, steam for use as a regeneration stream for a sorptive separation process can be produced by recovering a heat of adsorption as the first component or CO2 sorbs on and/or in the sorbent, and transferring the heat to a heat exchanger or vaporizer (configured internal of the CHP and/or external of the CHP) for vaporizing an aqueous or a water stream into a steam stream.

For chemical heat pumps using the first component or CO2 as the working fluid, the relative amounts of the first component or CO2 separated in a sorptive separation process versus the amount of the first component or CO2 used as a working fluid in a CHP process can be matched to reduce the pumping energy and estimated based upon the heat of adsorption of CO2, the heat of vaporization of water and a desired steam ratio used in the sorptive separator and sorptive separation process.

For example, a steam ratio or a ratio of an amount of steam used during a regenerating step of a sorptive separation process compared to a quantity of CO2 desorbed during the regenerating step can be between 2:1 to 4:1 mol of H2O/mol of CO2. A heat of adsorption of CO2 on a sorbent in a chemical heat pump may be about 36 kJ/mol, while a heat of vaporization of water is about 40 kJ/mol. Assuming about 50% of the heat is transferred from the sorbent in the CHP to generate steam while the rest is stored on the sorbent and internally recycled or lost, it can be desirable to use about 4 to 8 moles of CO2 cycling in the CHP for every 1 mole of CO2 separated in the sorptive separator and sorptive separation process. If it is desired to purify only one mole of CO2 through the CHP and CHP process, about 4 to 8 moles of CO2 cycling in the CHP for every 1 mole of CO2 separated plus an additional 3 to 7 moles of CO2 can be recovered from the sorptive separation process and added to the CHP process. A portion of the first component, CO2, or CHP product stream recovered from the CHP process can be recompressed and recycled to the CHP process while a portion of the first component, CO2, or CHP product stream can be recovered from the integrated sorptive separation process. For example, during one or more pressure equilibration steps of the CHP process or when switching from sorption at high pressure to desorption at low pressure in a vessel of the CHP process. In an embodiment, an integrated sorptive gas separation process and system can use the second component or water in the form of steam as the working fluid in a CHP and CHP process. An advantage is the second component or steam can have a higher heat of adsorption on a sorbent relative to the first component or CO2 thereby producing relatively more heat.

In an embodiment, if steam is used as a working fluid in a CHP process, steam for use as a regeneration stream for a sorptive separation process can be produced by: recovering steam from the CHP (during a pressure equilibration step of a CHP process); heating an aqueous solution or water in a heat exchanger within the chemical heat pump and/or external of the chemical heat pump using heat generated in the CHP during the sorption of steam, and/or recovering a CHP product stream from the vessel at a selected or reduced pressure and admitting the CHP product stream in a heat exchanger (separate of the CHP), a vaporizer, and/or a flash drum.

Sorptive Separation

In an embodiment of an integrated sorptive gas separation process, a sorptive separation process can comprise the following steps: a sorbing step (a), wherein a multi-component gas stream, with at least a first component, for example, an acid gas component such as carbon dioxide, is admitted as a feed stream into the sorptive separator, flowing the feed stream through the sorptive separator and contacting the feed stream with a sorbent in the sorptive separator; sorbing at least a portion of the first component of the feed stream in and/or onto the sorbent, separating the first component from the feed stream, and producing a first product stream depleted in a first component relative to the feed stream, and recovering the first product stream from the sorptive separator; and a regenerating step (b), wherein a regeneration stream with a second component into the sorptive separator is admitted, desorbing at least a portion of the first component sorbed in and/or onto the sorbent, producing a second product stream enriched in the first component relative to the feed stream, and recovering the second product stream from the sorptive separator.

In an embodiment, when the first component such as CO2 is used as a working fluid for a CHP and CHP process, at least a portion of the second product stream produced by or the first component such as CO2 recovered from the sorptive separator can be used for the CHP and CHP process by admitting the at least a portion of the second product stream or the first component such as CO2, recovered from the sorptive separator into the CHP and CHP process, or at least one vessel of the CHP In another embodiment, the at least a portion of the second product stream or a first component recovered from the second product stream can be admitted into the CHP at an elevated pressure by admitting the at least a portion of the second product stream into a compressor, recovering a compressed second product stream from the compressor, and admitting the compressed second product stream into the CHP and CHP process, or at least one vessel of the CHP

In further embodiments, the sorptive separation process can further comprise a conditioning step (c), wherein a conditioning stream, such as a gas stream with a low partial pressure of the second component or a relative humidity less than a relative humidity is admitted into the sorptive separator during regenerating step (b), desorbing at least a portion of the second component sorbed in and/or onto the sorbent, producing a third product stream enriched in the second component, for example, water which may be in the form of steam, relative to the influent stream or the feed stream, producing a third product stream enriched in the second component relative to the feed stream, and recovering the third product stream from the sorptive separator.

In an embodiment, when the second component, water, or steam is used as a working fluid for a CHP and a CHP process, at least a portion of the third product stream produced by the sorptive separator can be used for the CHP and the CHP process by admitting at least a portion of the third product stream into the CHP

Chemical Heat Pump

Chemical heat pump using a working fluid comprising the first component

In an embodiment of an integrated sorptive gas separation process, a chemical heat pump (CHP) process using a working fluid stream comprising the first component or CO2, can comprise the following steps:

(a) a first sorbing step: admitting the working fluid stream into a first circuit of a vessel of a CHP until a pressure in the first circuit comprising a heat pump sorbent is at a pressure equal to or greater than about a second pressure (or P2) and/or about a second temperature (or T2), sorbing the first component or CO2 from the working fluid in and/or on the heat pump sorbent, producing a heat of adsorption;

(b) a first de-pressurizing step: reducing the pressure in the first circuit, to a pressure equal to or less than about a first pressure (or P1 ), desorbing the first component or CO2 from the heat pump sorbent and forming a CHP product stream; and

(c) a vaporization step: admitting an aqueous liquid stream comprising the second component into a second circuit of the vessel, transferring the heat of adsorption produced in step (a) to the aqueous liquid stream comprising the second component for forming a regeneration stream, and recovering the regeneration stream from the second circuit of vessel and the CHP

In an embodiment, prior to and/or at the start of the first sorbing step or step (a), a pressure in the first circuit can be at a pressure equal to or less than about the first pressure (or P1 ) and/or about a first temperature (or T1 ). In a further embodiment, the first pressure (or P1 ) can be equal to or less than about atmospheric pressure. In a further embodiment, the first temperature (or T1 ) can be equal to or less than about 150°C, about 100°C, or less than about 80°C. The second pressure (or P2) can be greater than the first pressure (or P1 ) and/or the second temperature (or T2) can be greater than the first temperature (or T 1 ). The first sorbing step and the first depressurizing step can be repeated cyclically.

In an embodiment, during or after the vaporization step or step (c), the regeneration stream can be admitted into a sorptive separator during a regenerating step of a sorptive separation process. In an embodiment, after the first sorbing step or step (a), the process can comprise a second sorbing step: admitting the working fluid stream into the first circuit of the vessel of the CHP, until a pressure in the first circuit of the vessel is at a pressure equal to or greater than about a third pressure (or P3), sorbing the first component or CO2 from the working fluid in and/or on the heat pump sorbent, producing a heat of adsorption, transferring the heat of adsorption to the aqueous liquid stream for forming the regeneration stream. The third pressure (or P3) can be greater than the second pressure (or P2).

In an embodiment, after the second sorbing step, the process can comprise a first de-pressurizing step: reducing the pressure in the first circuit of the vessel to a pressure equal to or less than about a fourth pressure (or P4), desorbing the first component or CO2 from the heat pump sorbent, and producing a first pressure equalization stream or the CHP product stream. The fourth pressure (or P4) can be less than the third pressure (or P3).

In an embodiment, after the first pressurization step and before the second pressurization step, the process can comprise a pressure equalization step: admitting the first pressure equalization stream into the first circuit of the vessel of the CHP.

In an embodiment, after the first de-pressurizing step, the process can comprise a second de-pressurizing step: releasing the pressure in the first circuit of the vessel to a pressure equal to or less than about a fifth pressure (or P5) where the fifth pressure (or P5) can be less than the fourth pressure (or P4), desorbing the first component or CO2 from the heat pump sorbent producing at least one of the second pressure equalization stream or the CHP product stream, and transferring heat to the first circuit of the vessel and/or the heat pump sorbent and heating the first circuit of the vessel and/or the heat pump sorbent to a temperature equal to or greater than the first temperature (or T1 ). In an embodiment, the second sorbing step, first de-pressurizing step, and second de-pressurizing step can occur between the first sorbing step or step (a) and the first de-pressurizing step or step (c).

In a further embodiment, during the first de-pressurizing step and/or the second de-pressurizing step, the process can comprise a pressure equilibration step of cooling the heat pump sorbent to a third temperature (or T3) and reducing the pressure in the first circuit of the vessel and/or the heat pump sorbent to a pressure equal to or less than about the second pressure (or P2). The third temperature (or T3) can be less than the second temperature (or T2).

In the vaporizing step or step (c), the transferring of heat to the aqueous liquid stream can occur when a temperature of the first circuit of the vessel and/or heat pump sorbent is equal to or greater than about the second temperature (or T2).

In an embodiment, in the second de-pressurizing step, the process can comprise releasing the pressure in the first circuit of the vessel to a pressure equal to or less than about a fifth pressure (or P5), which can be achieved by pumping the second pressure equalization stream or the CHP product stream out of the first circuit and the vessel. In another embodiment, during the second de-pressurizing step, transferring heat to the first circuit of the vessel and/or the heat pump sorbent can be achieved by using a heat transfer fluid such as the aqueous liquid stream. In yet another embodiment, transferring heat to the first circuit of the vessel and/or the sorbent can be achieved by using a heat transfer fluid or the aqueous liquid stream at a temperature equal to or greater than a fourth temperature (or T4).

In an embodiment, in the second de-pressurizing step, reducing a pressure in the first circuit of the vessel to a pressure equal to or less than about an ambient pressure or about atmospheric pressure, for further desorbing components from the heat pump sorbent, further increasing the sorption capacity of the heat pump sorbent for the first component, and increasing the amount of heat transferred per cycle. In another embodiment, in the second de-pressurizing step recovering from a sorptive separator and/or a sorptive separation process a second product stream and admitting the second product stream into the first circuit of the vessel, and purging the first circuit of the vessel, producing a purge effluent stream. A pressure of the second product stream may be increased by admitting the second product stream into a compressor, fan, or blower, after recovering from the sorptive separator and prior to admitting into the first circuit of the vessel. In an embodiment, recovering the purge effluent stream from the first circuit of the vessel, recycling, and admitting the purge effluent stream into the sorptive separator. In an embodiment, in the first sorbing step or step (a), the working fluid stream comprising the first component such as CO2, can be sourced or recovered from a sorptive separator and/or a sorptive separation process, where the working fluid stream comprises a first concentration of the first component such as CO2. In another embodiment, in the first sorbing step or step (a), recovering a purge effluent stream from an outlet end of the first circuit of the vessel of the CHP which can be substantially opposite of an inlet end of the first circuit where the working fluid stream is admitted into the first circuit. In another embodiment in the first sorbing step or step (a), recovering a purge effluent stream from the outlet end of the first circuit when a pressure in the first circuit and/or the sorbent can be equal to or greater than about 1 bar absolute. In an embodiment, recovering the purge effluent stream from the first circuit of the vessel, recycling, and admitting the purge effluent stream into the sorptive separator. In one aspect, applying a vacuum to an outlet end of the first circuit of the vessel, or admitting a second product stream recovered from the sorptive separator as a purge stream into an inlet end of the first circuit of the vessel.

In an embodiment, the CHP can employ a plurality of vessels, for example, at least a first vessel and a second vessel. In a further embodiment, in the first sorbing step or step (a), increasing a pressure of in the first circuit and/or the sorbent of a first vessel can be by admitting at least one of a first pressure equalization stream and a second pressure equalization stream recovered from a first circuit of a second vessel of the chemical heat pump, wherein the at least one of first and second pressure equalization streams comprises a second concentration of the first component such as CO2. In a further embodiment, during a first de-pressurizing step and/or a second de-pressurizing step of a second vessel, at least one of a first pressure equalization stream and a second equalization stream can have a third concentration of the first component or CO2 prior to the first vessel reaching the second temperature (or T2) and the second pressure (or P2).

The pressure of the working fluid can be at a pressure greater than the third pressure. A compressor can be used to pressurize the working fluid or the second product stream recovered from the sorptive separator and/or sorptive separation process to a pressure greater than the third pressure. In embodiments, the second concentration of the first component can be less than the first concentration, and the third concentration of the first component can be greater than the first concentration.

Chemical Heat Pump Using H2O as a Working Fluid

In an embodiment of an integrated sorptive gas separation process, a chemical heat pump (CHP) process using a working fluid stream comprising the second component in a vapor form such as H2O in the form of steam, comprises the following steps:

(a) a first sorbing step: admitting a first portion of the working fluid stream into a first circuit of a vessel of a CHP where the first circuit of the vessel comprises a heat pump sorbent, sorbing the second component or water from the working fluid stream in and/or on the heat pump sorbent, and producing a heat of adsorption;

(b) a second sorbing step: admitting a second portion of the working fluid stream into the first circuit of the vessel, producing heat and increasing the temperature of the heat pump sorbent, and at least one of transferring heat from the vessel where the heat can be used for converting an aqueous liquid or a water stream into a steam stream, and storing the heat in the heat pump sorbent and/or the vessel for transferring the heat in a subsequent heat extraction step.

In an embodiment, the process further comprises during or after the second sorbing step (b), a heat extraction step (c): admitting a heat exchange fluid stream into a second circuit of the vessel, transferring heat from the vessel or first circuit of the vessel to the heat exchange fluid stream, and recovering the heat exchange fluid stream from the vessel for transferring heat for producing a regeneration stream for a sorptive separator.

In another embodiment, the working fluid can comprise a saturated steam stream with water droplets or water in the liquid phase. In another embodiment, admitting the working fluid comprising a saturated steam stream with water droplets or water in the liquid phase into the vessel, converting the water droplets or water in the liquid phase into steam by contacting the water droplets or water with the vessel and/or the sorbent with the heat stored during the second sorbing step (b), and recovering the steam from the vessel.

In an embodiment, after steps (b) or (c), a step (d) sealing and/or isolating the vessel, and reducing the pressure in the first circuit of the vessel. During or after steps (c) or (d), a step (e) recovering a steam stream from the first circuit of the vessel can be incorporated. The pressure of the steam stream can be increased by compressing the steam stream. After increasing the pressure of the steam stream, the steam stream can be cooled, reducing the temperature of the steam stream. In a step (f), admitting at least a portion of the steam stream from at least one of step (b) and (e) into a sorptive separator for regeneration of a sorbent in the sorptive separator.

In an embodiment, after step (e), reducing the pressure in the first circuit of the vessel and recovering a steam stream from the first circuit of the vessel, admitting the steam stream into a mechanical vapor recompression device, and increasing the pressure of the steam stream.

In an embodiment, repeating step (a) through step (f) with a plurality of the vessels where each vessel operates at a different step of the CHP process at a given time.

In an embodiment, in step (a) recovering the working fluid stream from a sorptive separator and/or a sorptive gas separation process. The working fluid stream can be a portion of a product stream or an effluent stream, such as a third product stream from a sorptive separator and/or sorptive gas separation process.

In an embodiment, in step (b) the second portion of the working fluid stream can have a concentration of steam equal to or greater than about 20% relative humidity (RH) and a pressure equal to or greater than about 2 bar absolute. The second portion of the working fluid stream can be a portion of a product stream or an effluent stream, such as a third product stream from the sorptive separator and/or a product stream from a conditioning step of the sorptive gas separation process. The pressure of the third product stream may be increased by compressing the third product stream prior to admitting into the CHP and/or vessel.

In step (d) the reduction in the pressure of the working fluid in the vessel can be achieved by at least one of equalizing the pressure of the vessel with another vessel of the CHP during a pressure equilibration step, and/or by pumping the working fluid or steam stream using a mechanical device, an ejector, or any suitable device for transferring momentum to the gas molecules in the vessel in a certain direction.

In an embodiment, an integrated sorptive gas separation process for separating a first component from a multi-component gas stream can comprise:

(a) admitting the multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, sorbing the first component on and/or in the sorbent, recovering a first product stream depleted in the first component relative to the feed stream, admitting a regeneration stream comprising a second component into the sorptive separator, desorbing the first component from the sorbent, and recovering a second product stream from the sorptive separator, wherein the second product stream can be enriched in the first component relative to the feed stream;

(b) admitting at least a portion of the second product stream into a first circuit of a vessel of a chemical heat pump, wherein the first circuit of the vessel can be at a first pressure prior to admitting the at least a portion of the second product stream, increasing the pressure of the first circuit of the vessel to a second pressure, sorbing the first component on and/or in a heat pump sorbent in the first circuit of the vessel thus producing heat;

(d) transferring the heat produced in step (b) to an aqueous liquid stream comprising a second component in a second circuit of the vessel of the chemical heat pump and converting at least a fraction of the liquid stream into a vapor comprising the second component or steam, for forming at least a portion of the regeneration stream, wherein in step (c), the chemical heat pump product stream is at least periodically enriched in the first component relative to the second product stream.

In an embodiment, prior to step (a), the process can further comprise contacting the feed stream with a heat exchanger or direct contact cooler, recovering and transferring heat from the feed stream to the chemical heat pump. In embodiments, at least one of: the first component can be CO2 or a C2⁺ hydrocarbon; the second component can be water; the multi-component stream can be a flue gas stream, ambient air, an air stream conditioned by a heating, ventilation, and air conditioning (HVAC) device, a bio-methane gas stream, a natural gas stream, a hydrocarbon gas stream, a gas stream with H2, CO and CO2; at least one of the first pressure can be in a range of about 20 to 100 kPa absolute and the second pressure can be in a range of about 150 and 500 kPa absolute; at least one of the sorbent in the sorptive separator and the heat pump sorbent in the first circuit of the vessel in the chemical heat pump can be at least one of a metal organic framework, a zeolite, an activated carbon, a physisorbent, an absorbent in a liquid or semi-liquid phase, or an absorbent supported on a porous solid; and the chemical heat pump comprises a plurality of vessels.

(a) admitting the multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, sorbing the first component one and/or in the sorbent in the sorptive separator, recovering a first product stream depleted in the first component relative to the feed stream, admitting a regeneration stream comprising a second component into the sorptive separator, desorbing the first component from the sorbent in the sorptive separator, adsorbing the second component on and/or in the sorbent in the sorptive separator, recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator, admitting a conditioning stream into the sorptive separator wherein the conditioning stream has a partial pressure of the second component less than a partial pressure of the second component around the sorbent in the sorptive separator measured at the end of the recovery of the second product stream, desorbing the second component from the sorbent in the sorptive separator to form a third product stream enriched in the second component relative to the conditioning stream, and recovering the third product stream from the sorptive separator;

(b) admitting at least a portion of the third product stream into a first circuit of a vessel of a chemical heat pump, wherein the first circuit of the vessel can be at a pressure equal to or less than a first pressure and a first temperature before admitting the portion of the third product stream, increasing the pressure of the first circuit of the vessel to equal or greater than a second pressure, sorbing the second component on and/or in a heat pump sorbent in the first circuit of the vessel, producing heat and increasing the temperature within the first circuit of the vessel to equal or greater than a second temperature;

In an embodiment of the integrated sorptive gas separation process, the third product stream can have a composition of the second component of equal to or greater than about 20% by volume. In embodiments, the integrated sorptive gas separation process further comprises at least one of: increasing a pressure of the third product stream relative to a pressure of the third product stream recovered from the sorptive separator before admitting it in the chemical heat pump, wherein the step of admitting the third product stream into the first circuit of the first vessel of the chemical heat pump releases heat and increases a temperature in the first circuit of the first vessel equal to or greater than a third temperature; compressing the chemical heat pump product stream and combining the chemical heat pump product stream with the regeneration stream for admitting into the sorptive separator in step (a); admitting the chemical heat pump product stream into at least one of a flash drum and a mechanical vapor recompression device, recovering the chemical heat pump product stream from at least one of the flash drum and the mechanical recompression device and combining the chemical heat pump product stream with the regeneration stream for admitting into the sorptive separator in step (a), wherein the first component can be CO2 or a C2⁺ hydrocarbon, the second component can be water, the multi-component stream can be a flue gas stream, ambient air, an air stream conditioned by a heating, ventilation, and air conditioning (HVAC) device, a bio-methane gas stream, a natural gas stream, a hydrocarbon gas stream, a gas stream with H2, CO and CO2, wherein at least one of the first pressure can be in a range of about 20 to 100 kPa absolute and the second pressure can be in a range of about 150 and 500 kPa absolute, wherein at least one of the sorbent in the sorptive separator and the heat pump sorbent in the first circuit of the vessel in the chemical heat pump can be at least one of a metal organic framework, a zeolite, an activated carbon, a physisorbent, an absorbent in a liquid or semi-liquid phase, or an absorbent supported on a porous solid; and the chemical heat pump comprises a plurality of vessels.

An integrated sorptive gas separation system using a chemical heat pump to produce a regeneration stream for a sorptive separator can reduce the energy consumption relative to conventional integrated sorptive gas separation processes using a boiler to produce a steam stream as a regeneration stream. Furthermore, the chemical heat pump can also offer the additional benefit of producing a product stream with an increased concentration of the first component relative to conventional processes of using a boiler to produce the regeneration stream.

Integrated Sorptive Gas Separation System

Referring to Fig. 1 , an embodiment of an integrated sorptive gas separation system 1 with a sorptive separator and a chemical heat pump (CHP) with a plurality of vessels is shown. In embodiments, the integrated sorptive gas separation system 1 uses a working fluid comprising a first component, such as CO2, for the CHP. A sorptive separator 160 comprising a plurality of sorbent contactors (not shown in Fig. 1 ) is fluidly connected to a multi-component feed source (not shown in Figure 1 ), for admitting a multi-component gas stream as a feed stream 101 b comprising the first component into sorptive separator 160. Each sorbent contactor of sorptive separator 160 comprises a sorbent (not shown in Fig. 1 ). A sorptive separation process using swing mechanisms, such as but not limited to, temperature swing, partial pressure swing, and/or moisture swing can be used for sorptive separator 160. During a sorbing step of a sorptive separation process, feed stream 101 b contacts the sorbent within sorptive separator 160, where the first component in feed stream 101 b sorbs in and/or onto the sorbent, producing a first product stream 161 depleted in the first component relative to feed stream 101 b. First product stream 161 can be recovered from sorptive separator 160 and the integrated sorptive gas separation system 1. Sorptive separator 160 is fluidly connected to receive and admit a regeneration stream, for example, a steam stream 121 , into sorptive separator 160, to contact the sorbent and desorb the first component sorbed on and/or in the sorbent thereby producing a second product stream 123 enriched in the first component relative to feed stream 101 b. Second product stream 123 can be recovered from sorptive separator 160 and the second component in second product stream 123 can be substantially removed and cooled.

In an embodiment, sorptive separator 160 is fluidly connected to admit second product stream 123 into a chemical heat pump or a CHP 400 as the working fluid. In another embodiment, sorptive separator 160 is fluidly connected to admit second product stream 123 into CHP 400 via a compressor 300 for increasing the pressure of second product stream 123 and producing a second product stream 301 . Compressor 300 can be fluidly connected to receive the second product stream 123 from sorptive separator 160 via a heat exchanger (not shown in Fig. 1 ) to reduce the temperature of second product stream 123 prior to admitting into compressor 300.

In an embodiment, during a conditioning step of the sorptive separation process, sorptive separator 160 is fluidly connected to a conditioning source (not shown in Fig. 1 ) to admit a conditioning stream 103 with a low partial pressure of the second component into sorptive separator 160 to contact the sorbent, thereby desorbing the second component sorbed on and/or in the sorbent, and producing a third product stream 163 enriched in the second component relative to feed stream 101 b and conditioning stream 103. Third product stream 163 can be recovered from sorptive separator 160 and integrated sorptive gas separation system 1.

Fig. 1 depicts an integrated sorptive gas separation system 1 and CHP 400 with a plurality of vessels. However, an integrated sorptive gas separation system and CHP can have a single vessel. CHP 400 comprises a first vessel 401 and a second vessel 402, each vessel with a heat pump sorbent in a first circuit (both not shown in Fig. 1 ) and operable using a swing mechanism, for example, a pressure swing. CHP 400 is fluidly connected to compressor 300 for admitting second product stream 301 into CHP 400 as a working fluid, and alternatively into a first circuit (not shown in Fig. 1 ) in first vessel 401 and a first circuit (not shown in Fig. 1 ) in second vessel 402 during one or more pressurization steps for first vessel 401 and second vessel 402. The first component in second product stream 301 can be sorbed in and/or on the heat pump sorbent in first vessel 401 and second vessel 402, producing heat. In an embodiment, sorptive separator 160 can be fluidly connected to recover a purge effluent stream 102 from the first circuit in first vessel 401 , the first circuit in second vessel 402, and CHP

400 for admitting into sorptive separator 160 and separating the first component from purge effluent stream 102. The pressure of purge effluent stream 102 can be reduced prior to admittance into sorptive separator 160. At the end of the pressurization step, the recovery of purge effluent stream 102 can be terminated, for example, by closing valves configured at an outlet of the first circuit in first vessel 401 and an outlet of the first circuit in second vessel 402. In an embodiment, the first circuit in first vessel 401 and the first circuit in second vessel 402 can be fluidly connected to recover and admit a pressure equalization stream between the first circuit in first vessel 401 and the first circuit in second vessel 402, and/or the first circuit in second vessel 402 and the first circuit in first vessel 401 .

In an embodiment, first vessel 401 comprises a second circuit (not shown in Fig. 1 ) and second vessel 402 comprises a second circuit (not shown in Fig. 1 ), wherein the second circuit in first vessel 401 and the second circuit in second vessel 402 are fluidly connected to a liquid source (not shown in Fig. 1 ) to admit an aqueous stream such as a water stream 403 into the second circuits of first vessel 401 and second vessel 402 where the second circuits of first vessel 401 and second vessel 402 can be fluidly connected and configured as a loop. The first circuits of first vessel 401 and second vessel 402 can be substantially fluidly separate from, but thermally connected to the second circuits in first vessel 401 and second vessel 402. The heat of adsorption released during the sorbing steps of the CHP in the first circuits of first vessel 401 and second vessel 402 can be transferred to the first circuits of first vessel

401 and second vessel 402, converting the aqueous fluid or water stream 403 in the second circuits of first vessel 401 and second vessel 402 into a gas phase such as a steam stream 405. CHP 400, the second circuit of first vessel 401 and the second circuit of second vessel 402 is fluidly connected to admit steam stream 405 or steam stream 121 into sorptive separator 160 as a regeneration stream.

In embodiments, the second circuit in first vessel 401 and the second circuit in second vessel 402 are fluidly connected to recover and admit the aqueous fluid or water stream 403 between first vessel 401 and second vessel 402, for transferring heat via water stream 403 between first vessel 401 and second vessel 402. For example, as first vessel 401 performs a sorbing step of a CHP process a heat of adsorption can be released and transferred via water stream 403 from first vessel 401 to second vessel 403 performing a depressurization step such as a first depressurization or a second de-pressurizing step of the CHP process, and vice versa.

In embodiments, a stream conditioner 120 can be fluidly connected to CHP 400, the second circuit of first vessel 401 , the second circuit of second vessel 402, and sorptive separator 160, for adjusting, regulating, and/or controlling at least one of the pressure and the temperature of steam stream 405 to form and admit steam stream 121 into sorptive separator 160.

In embodiments, first circuit of first vessel 401 , first circuit of second vessel 402, CHP 400, and integrated sorptive gas separation system 1 can be fluidly connected to recover a CHP product stream 410 at a reduced pressure during a depressurization step relative to a pressure in the first circuits of first vessel 401 and second vessel 402 during their respective sorbing step. CHP product stream 410 can at least periodically have an elevated concentration of the first component, such as CO2, relative to second product stream 123 and second product stream 301 . CHP 400, first circuit in first vessel 401 and first circuit in second vessel 401 can be fluidly connected to compressor 300 for recovering and admitting a portion of CHP product stream 410 as a recycle product stream 409, into compressor 300. In an embodiment, a supplemental steam stream 122 can be combined with steam stream 121 , if the quantity of steam produced by CHP is insufficient and additional steam is desired to carry out a regenerating step in sorptive separator 160. In an embodiment, first vessel 401 comprises a second circuit (not shown in Fig. 1 ) and second vessel 402 comprises a second circuit (not shown in Fig. 1 ), wherein the second circuit in first vessel 401 can be fluidly connected to the second circuit in second vessel 402 for flowing a liquid heat exchange medium such as a water stream 403 to transfer heat in and out of first vessel 401 and second vessel 402 at different steps of the CHP process. The heat may be used for the CHP process and/or to produce a regeneration stream or a steam stream 121 for sorptive separator 160.

In an embodiment, first circuit of first vessel 401 and/or first circuit of second vessel 402 can be fluidly connected to sorptive separator 160 for recovering a purge effluent stream 102 from the first circuit of first vessel 401 and/or first circuit of second vessel 402, recycling, and admitting purge effluent stream 102 into sorptive separator 160. In an embodiment, first circuit of first vessel 401 and/or first circuit of second vessel 402 is fluidly connected to recover purge effluent stream 102 from first circuit of first vessel 401 and/or first circuit of second vessel 402, CHP 400, and integrated sorptive gas separation system 1 .

In an embodiment, integrated sorptive gas separation system 1 comprises a heat exchanger such as a direct contact cooler or a DCC 110 fluidly connected to a multicomponent fluid stream source (not shown in Fig. 1 ) and sorptive separator 160 for reducing the temperature of a feed stream 101a and producing feed stream 101 b. Heat recovered from DCC 110 can be used to assist in producing the regeneration stream or a steam stream for sorptive separator 160. In an embodiment, integrated sorptive gas separation system 1 comprises a heat exchanger 170 fluidly connected to recover third product stream 163 from sorptive separator 160 and admitting third product stream 163 into CHP 400, first circuit of first vessel 401 and first circuit of second vessel 402. Heat exchanger 170 can recover heat and reduce the temperature of third product stream 163, where the heat recovered from third product stream 163 can be used to assist in producing the regeneration stream or a steam stream for sorptive separator 160. Water recovery as a liquid from third product stream 163 using a chemical heat pump can enable large amounts of heat to be upgraded from about 20°C to 40°C, up to about 70°C to 90°C, as the steam partial pressure in third product stream 163 is typically greater than 20 kPa. Cooling fluid loops (not shown in Fig. 1 ) can be thermally connected to the water stream 403.

Fig. 2a illustrates an exemplary configuration of first vessel 401 and second vessel 402 of CHP 400 shown in integrated sorptive gas separation system 1 in Fig. 1. Fig. 2b illustrates a cross-section view of first vessel 401 shown in Fig. 2a. Second product stream 301 can be admitted into a first circuit 712 to come into contact with a heat pump sorbent 711 to release a heat of adsorption. Heat pump sorbent 711 can be coated on a barrier material such as a tube wall 710. The heat can transfer from sorbent 711 through tube wall 710 to a second circuit 713 for converting a water stream 403 to steam stream 405, or alternatively for water stream 403 to transfer and convey heat away from first vessel 401 to produce a regeneration stream such as a steam stream for a sorptive separator. A vessel can be configured with other suitable configurations which can be similar to heat exchanger (HEX) configurations including, for example, a plate HEX.

The coefficient of efficiency of the CHP is affected by the temperature differential between a steam generation temperature (T_g) (steam generation temperature) and a heat recovery temperature (T_r), the heat capacity of the heat pump sorbent and structure creating the first and second circuits, the heat pump sorbent cycle sorption capacity, and the heat of adsorption of the first component or the steam. Reducing a total heat capacity of the stationary solids of the CHP, such as the barrier layer between the first and second circuits and heat pump sorbent, beneficially assists in reducing the amount of heat that is required to be internally recycled and to maximize the amount of usable heat from the cycle used for steam production. As the mechanical energy to compress the working fluid can be controlled by the target pressure and the quantity of the first component or steam used in each cycle, maximizing usable heat per cycle increases the heat pump coefficient of performance.

Referring to Fig. 3, in an embodiment, the integrated sorptive gas separation system 2 with a sorptive separator 160 and a chemical heat pump (CHP) 400 with a plurality of vessels using a working fluid comprising the second component in a vapor form such as H2O in the form of steam, is shown. In embodiments, the integrated sorptive gas separation system 2 is similar to integrated sorptive gas separation system 1 shown in Fig. 1 , but configured to use a different working fluid. In Fig. 3, sorptive separator 160 is fluidly connected to recover and admit third product stream 163 into CHP 400, first circuit of first vessel 401 and first circuit of second vessel 402. Integrated sorptive gas separation system 2 and sorptive separator 160 are fluidly connected to an end user (not shown in Fig. 3) to recover second product stream 123.

Referring to Fig. 4, in an embodiment, the integrated sorptive gas separation system 3 with a sorptive separator 160 and a chemical heat pump (CHP) 400 with a plurality of vessels using a working fluid comprising the second component in a vapor form such as H2O in the form of steam, is shown. In embodiments, the integrated sorptive gas separation system 3 is similar to the integrated sorptive gas separation system 2 shown in Fig. 3, however CHP 400 produces a CHP product stream 411 which can be used as a regeneration stream for sorptive separator 160. Integrated sorptive gas separation system 3 is configured such that sorptive separator 160 is fluidly connected to CHP 400, the first circuit of first vessel 401 and the first circuit of second vessel 402, for recovering and admitting CHP product stream 411 comprising the second component such as H2O in the form of steam, as a regeneration stream into sorptive separator 160. In alternative embodiments, first vessel 401 and second vessel 402 comprises a first circuit only.

Referring to Fig. 5, in an embodiment, an integrated sorptive gas separation system 4 with a sorptive separator 160, a chemical heat pump (CHP) 400 with a plurality of vessels using a working fluid comprising the second component in a vapor form such as H2O in the form of steam, and additional devices for producing the regeneration stream for sorptive separator 160 is shown. Integrated sorptive gas separation system 4 is similar to integrated sorptive gas separation system 3 shown in Fig. 4, however integrated sorptive gas separation system 4 comprises and is configured with a flash drum 180, a mechanical vapor recompressor (MVR) 172 and a mechanical vapor recompressor (MVR) 171 for producing steam stream 405. In an embodiment of an integrated sorptive gas separation system, a sorptive separator 160 is fluidly connected to receive a steam stream 405 from at least one of CHP 400 via MVR 171 , CHP 400 via flash drum 180, CHP 400 via MVR 172 and flash drum 180. In an embodiment, an integrated sorptive gas separation system for separating a first component from a multi-component gas stream can comprise: a sorptive separator with a sorbent, a feed port for admitting the multicomponent gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream from the sorptive separator, a regeneration port for admitting a regeneration stream into the sorptive separator, a second product port for recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator, wherein the feed port and first product port can be fluidly connected and the regeneration port and the second product port can be fluidly connected; and a chemical heat pump comprising at least one vessel with a first circuit having a heat pump sorbent and a second circuit, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream, a liquid inlet port fluidly connected to the second circuit of the vessel for admitting an aqueous liquid stream or a water stream into the second circuit, and a fluid outlet port fluidly connected to the second circuit of the vessel for recovering the aqueous liquid stream or a stream from the second circuit.

In embodiments, the integrated sorptive gas separation system can have a water evaporator or a heat exchanger for converting an aqueous liquid stream comprising water into a stream comprising steam, the water evaporator or the heat exchanger comprising a liquid inlet port fluidly connected to a steam outlet port, a heating inlet port fluidly connected to a heating outlet port, wherein the liquid inlet port can be fluidly connected to an aqueous liquid supply, the stream outlet port of the water evaporator or the heat exchanger can be fluidly connected to the regeneration port of the sorptive separator, and the fluid outlet port of the vessel can be fluidly connected to the heating inlet port of the water evaporator or the heat exchanger. The heat pump sorbent in the vessel of the chemical heat pump can be configured in the form of a film, a layer or a sheet, and can be interposed between the first circuit and the second circuit of the vessel. The vessel of the chemical heat pump can have a diffusion barrier fluidly separating the first circuit of the vessel and the heat pump sorbent from the second circuit of the vessel, and in contact and thermally connected to the heat pump sorbent. The first circuit of the vessel can have a first circuit volume and the second circuit of the vessel can have a second circuit volume where the first circuit volume and the second circuit volume are each equal to or less than about 30% of a volume in the vessel. The heat pump sorbent can be configured in a form of a film, a layer, or a sheet, with a thickness in a range of about 0.1 to 1 mm. The heat pump sorbent can have a surface area of the film, layer or sheet, per volume of the heat pump sorbent in a range of about 250 m²/m³ to 2500 m²/m³. The chemical heat pump can have a plurality of vessels.

In an embodiment, an integrated sorptive gas separation system for separating a first component from a multi-component gas stream can comprise: a sorptive separator comprising a sorbent, a feed port for admitting the multi-component gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream, a regeneration port for admitting a regeneration stream into the sorptive separator, a second product port for recovering a second product stream enriched in the first component relative to the feed stream, a conditioning port for admitting a conditioning stream into the sorptive separator, and a third product port for recovering a third product stream from the sorptive separator, wherein the feed port and first product port, can be fluidly connected, the regeneration port and the second product port can be fluidly connected, and the conditioning port and the third product port can be fluidly connected; and a chemical heat pump comprising at least one vessel with a first circuit having a heat pump sorbent, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream; wherein the third product port can be fluidly connected to the working fluid port.

In embodiments, the integrated sorptive gas separation system can have a water evaporator or a heat exchanger for converting an aqueous liquid stream comprising water into a stream comprising steam, the water evaporator or the heat exchanger comprising a liquid inlet port fluidly connected to a steam outlet port, a heating inlet port fluidly connected to a heating outlet port, wherein the liquid inlet port can be fluidly connected to an aqueous liquid supply, the stream outlet port of the water evaporator or the heat exchanger can be fluidly connected to the regeneration port of the sorptive separator, and the fluid outlet port of the vessel can be fluidly connected to the heating inlet port of the water evaporator or the heat exchanger. The heat pump sorbent in the vessel of the chemical heat pump can be configured in the form of a film, a layer or a sheet, and can be interposed between the first circuit and a second circuit of the vessel. In embodiments, the vessel of the chemical heat pump can have a diffusion barrier fluidly separating the first circuit of the vessel and the sorbent from the second circuit of the vessel and can be thermally contacted to the sorbent. The first circuit of the vessel can have a first circuit volume and the second circuit of the vessel can have a second circuit volume wherein the first circuit volume and the second circuit volume are each equal to or less than about 30% of a volume in the vessel. The heat pump sorbent can be configured in a form of a film, a layer, or a sheet, with a thickness in a range of about 0.1 to 1 mm, and having a surface area of the film, layer, or sheet, per volume of the heat pump sorbent can be in the range of about 250 m²/m³ to 2500 m²/m³. The chemical heat pump can have a plurality of vessels.

In an embodiment, a vessel of a chemical heat pump can comprise a vessel; a heat pump sorbent; a first circuit; and a second circuit, wherein the heat pump sorbent can be configured as a film, layer, or sheet, having a thickness in a range of 0.1 and 1 mm, and interposed between the first circuit and the second circuit. The heat pump sorbent, in embodiments, can have a surface area per volume in a range of 250m²/m³ and 2500 m²/m³, and have a heat capacity equal to or greater than 50% of a heat capacity of the vessel when the first circuit and second circuit are filled with a gas.

Table 1 provides modeled estimates of various parameters for various streams of the integrated sorptive gas separation system 1 shown in Fig. 1. As shown, the amount of the second component or CO2 in recycle product stream 409 recycled through compressor 300 is a multiple of the amount of the second component or CO2 recovered in second product stream 123 from sorptive separator 160 to provide a desired quantity of the regeneration stream or steam to the sorptive separation process. In embodiments, if an additional quantity of steam is desired, steam can be provided, for example, by a different source for supplemental steam stream 122.

Table 1 : Estimates of flow rates, compositions, and pressures for various streams of the integrated sorptive gas separation system shown in Fig. 1 .

Fig. 6a is a schematic diagram of a vacuum-pressure swing adsorption (VPSA) or vacuum-pressure swing chemical heat pump (CHP) process with at least seven steps where each step can be conducted in a single vessel and each step can be conducted substantially simultaneously with at least seven vessels. The CHP process uses a working fluid comprising the first component.

Fig. 6b is a graphic representation of the pressures and temperatures for the sorbent as a function of cycle time for a vessel through different chemical heat pump process steps. As shown, in embodiments, in a first or a first pressurization step, a working fluid stream comprising an elevated concentration of the second component or CO2, for example, a second product stream 801 at elevated pressure recovered from a sorptive separator and a sorptive separation process, is admitted into a first vessel 821 where the second component or CO2 is sorbed and loaded on and/or in a heat pump sorbent in first vessel 821 while a purge effluent stream 802a depleted in the second component or CO2 relative to the second product stream 801 is recovered from first vessel 821 . In a fifth or a first de-pressurizing step, a pressure equalization stream 803 can be recovered from a fifth vessel 825 and admitted into a second vessel 822 conducting a second or a second pressurization step. A purge effluent stream 802b depleted in the second component or CO2 relative to the second product stream 801 can be recovered from second vessel 822 during the second pressurization step. Purge effluent streams 802a and 802b can be recycled and admitted into sorptive separator 160 for separation and capture of the first component. A third vessel 823 can conduct a third or a third pressurization step, while a fourth vessel 824 can conduct a fourth or a fourth pressurization step where the pressure of a second recycle stream 809b admitted into third vessel 823 and a first recycle stream 809a admitted into fourth vessel 824 can be further increased incrementally while heat is recovered and transferred to an aqueous fluid to produce steam. During the fourth pressurization step, the heat pump sorbent can reach a sorbent equilibration where the loading of the second component on and/or in the heat pump sorbent is substantially about equilibrium with the sorptive capacity of the heat pump sorbent at a designed target pressure. During a fifth or first de-pressurizing step, a pressure in fifth vessel 825 can be released or de-pressurized to produce pressure equalization stream 803. During a sixth or second de-pressurizing step in a sixth vessel 826, the pressure in sixth vessel 826 is released to form a product stream 811 . During a seventh or third de-pressurizing step in a seventh vessel 827, the pressure in seventh vessel 827 is released to form a product stream 810. During the sixth or second de-pressurizing step in sixth vessel 826 and seventh or third depressurizing step in seventh vessel 827, the steps can be started initially under near adiabatic conditions with heat added and transferred into the vessels and heat pump sorbent in the vessels. This can be performed by flowing a heat transfer fluid, such as an aqueous stream, in a second circuit of a plurality of vessels to remove heat from one or more vessels and adding heat to one or more vessels. During the sixth and seventh steps, product stream 811 can be divided into two portions, a starting or an first portion 811a and an ending or second portion 811 b, and product stream 810 can be divided into two portions, a starting or an first portion 810a and an ending or second portion 810b, where the first portions 811a and 810a of product streams 811 and 810 recovered from the vessels comprises a reduced purity or concentration of the second component or CO2 relative to the ending or second portion of the product stream during these steps. The first portion 811a and first portion 810a can be recycled as pressure equalization streams to third vessel 823 performing the third pressurization step and fourth vessel 824 performing the fourth pressurization step respectively. The second portion 811 b and second portion 811 b can be recovered as product stream high in purity or concentration in the first component from the chemical heat pump and integrated sorptive gas separation system. Fig. 6b is a graph showing the corresponding temperatures and pressures of a vessel of a chemical heat pump during each step of the pressure swing adsorption (V-PSA) or vacuum-pressure swing chemical heat pump (CHP) process shown in Fig. 6a. The y-axis represents pressure and temperature, while the x-axis represents time.

Pressure plot 830 represents the pressure and temperature plot 831 represents the temperature during a first step or a first pressurization step 832, a second step or a second pressurization step 833, a third step or a third pressurization step 834, a fourth step or a fourth pressurization step 835, a fifth step or a first depressurizing step 836, a sixth step or a second de-pressurizing step 837, and a seventh step or a third de-pressurizing step 838. Line 839 represents atmospheric pressure or 1 bar absolute. During the steam generation steps (in Fig. 6b, second pressurization step 833, third pressurization step 834, and fourth pressurization step 835) and heat recovery steps (in Fig. 6b, second de-pressurizing step 837 and third de-pressurizing step 838), the temperature of the sorbent can be substantially isothermal while second component or CO2 is adsorbed or desorbed from the heat pump sorbents. During intermediate steps (in Fig. 6b first pressurization step 832and first de-pressurizing step 836), the temperature of the sorbent increases to the steam generation temperature T_g or decreases to the heat recovery temperature T_r through an increase or decrease in CO2 loading on the sorbent.

While the temperature swing of the sorbent between these two temperatures T_g and T_r uses a significant fraction of the sorbent cyclic capacity, most of this energy being stored on the solid can be recovered during the pressure equilibration step, thus reducing the overall energy cost of the process.

Fig. 7 is a graph showing the purity or concentration of the first component of a working fluid of a pressure swing adsorption (V-PSA) or vacuum-pressure swing chemical heat pump (CHP) process. The y-axis represents the concentration of the first component in molar %, while the x-axis represents time or steps of the CHP process. Concentration plot 840 is shown during a pressurization step 841 , representing the concentration of the working fluid or a second product stream from a sorptive separator admitted in the CHP and vessels (for example, a first and/or a second pressurization step), during a starting or a first portion 842 of a de-pressurization step (for example, a first and/or a second de-pressurization step), and an ending or a second portion 843 of the de-pressurization step. Concentration plot 840 shows a decreased concentration of the first component during first portion 842 and an increased concentration of the first component during second portion 843 relative to the concentration of the working fluid stream admitted into the vessel of the CHP during pressurization step 841 . Second portion 843 illustrates a benefit of using a CHP configured to use a working fluid recovered from the sorptive separator with the first component in an integrated sorptive gas separation system resulting in producing a chemical heat pump product stream with an elevated concentration of the first component relative to a sorptive separation system with only a sorptive separator, while generating useful heat.

Claims

Claims:

1 . An integrated sorptive gas separation process for separating a first component from a multi-component gas stream, the process comprising:

(a) admitting the multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, sorbing the first component on and/or in the sorbent, recovering a first product stream depleted in the first component relative to the feed stream, admitting a regeneration stream comprising a second component into the sorptive separator, desorbing the first component from the sorbent, and recovering a second product stream from the sorptive separator, wherein the second product stream is enriched in the first component relative to the feed stream;

(b) admitting at least a portion of the second product stream into a first circuit of a vessel of a chemical heat pump, wherein the first circuit of the vessel is at a first pressure prior to admitting the at least a portion of the second product stream, increasing the pressure of the first circuit of the vessel to a second pressure, sorbing the first component on and/or in a heat pump sorbent in the first circuit of the vessel for producing heat;

(d) transferring the heat produced in step (b) to an aqueous liquid stream comprising a second component in a second circuit of the vessel of the chemical heat pump, and converting at least a fraction of the liquid stream into a vapor comprising the second component or steam, for forming at least a portion of the regeneration stream, wherein in step (c), the chemical heat pump product stream is at least periodically enriched in the first component relative to the second product stream.

2. The process of claim 1 , further comprising prior to step (a), contacting the feed stream with a heat exchanger or direct contact cooler, recovering and transferring heat from the feed stream to the chemical heat pump.

3. An integrated sorptive gas separation process for separating a first component from a multi-component gas stream, the process comprising:

(a) admitting the multi-component gas stream as a feed stream into a sorptive separator comprising a sorbent, sorbing the first component on and/or in the sorbent in the sorptive separator, recovering a first product stream depleted in the first component relative to the feed stream, admitting a regeneration stream comprising a second component into the sorptive separator, desorbing the first component from the sorbent in the sorptive separator, adsorbing the second component on and/or in the sorbent in the sorptive separator, recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator, admitting a conditioning stream into the sorptive separator wherein the conditioning stream has a partial pressure of the second component less than a partial pressure of the second component around the sorbent in the sorptive separator measured at the end of recovery of the second product stream, desorbing the second component from the sorbent in the sorptive separator to form a third product stream enriched in the second component relative to the conditioning stream, and recovering the third product stream from the sorptive separator;

(b) admitting at least a portion of the third product stream into a first circuit of a vessel of a chemical heat pump wherein the first circuit of the vessel is at a pressure equal to or less than a first pressure and a first temperature before admitting the portion of the third product stream, increasing the pressure of the first circuit of the vessel to equal or greater than a second pressure, sorbing the second component on and/or in heat pump sorbent in the first circuit of the vessel, producing heat and increasing the temperature within the first circuit of the vessel to equal or greater than a second temperature;

4. The process of claim 3, wherein the third product stream has a composition of the second component of equal to or greater than 20% by volume.

5. The process of claim 4, further comprising, increasing a pressure of the third product stream relative to a pressure of the third product stream recovered from the sorptive separator before admitting it in the chemical heat pump.

6. The process of claims 4 or 5, wherein the step of admitting the third product stream into the first circuit of the first vessel of the chemical heat pump further comprises releasing heat and increasing a temperature in the first circuit of the first vessel.

7. The process of any one of claims 3 to 6, further comprising compressing the chemical heat pump product stream and combining the chemical heat pump product stream with the regeneration stream for admitting into the sorptive separator in step (a).

8. The process of any one of claims 3 to 7, further comprising admitting the chemical heat pump product stream into at least one of a flash drum and a mechanical vapor recompression device, recovering the chemical heat pump product stream from at least one of the flash drum and the mechanical recompression device and combining the chemical heat pump product stream with the regeneration stream for admitting into the sorptive separator in step (a).

9. The process of claims 1 or 3, wherein the first component is CO2 or a C2⁺ hydrocarbon.

10. The process of any one of claims 1 , 3, or 4, wherein the second component is water.

11 . The process of claims 1 or 3, wherein the multi-component stream is a flue gas stream, ambient air, an air stream conditioned by a heating, ventilation, and air conditioning device, a bio-methane gas stream, a natural gas stream, a hydrocarbon gas stream, a gas stream with H2, CO and CO2.

12. The process of any one of claims 1 or 3, wherein at least one of the first pressure is between 20 and 100 kPa absolute and the second pressure is between 150 and 500 kPa absolute.

13. The process of any one of claims 1 to 11 , wherein at least one of the sorbent in the sorptive separator, and the heat pump sorbent in the first circuit of the vessel in the chemical heat pump is at least one of a metal organic framework, a zeolite, an activated carbon, a physisorbent, an absorbent in a liquid or semi-liquid phase, or an absorbent supported on a porous solid.

14. An integrated sorptive gas separation system for separating a first component from a multi-component gas stream, the system comprising:

(a) a sorptive separator comprising: a sorbent, a feed port for admitting the multi-component gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream from the sorptive separator, a regeneration port for admitting a regeneration stream into the sorptive separator, and a second product port for recovering a second product stream enriched in the first component relative to the feed stream from the sorptive separator, wherein the feed port and first product port is fluidly connected and wherein the regeneration port and the second product port is fluidly connected; and

(b) a chemical heat pump comprising: at least one vessel with a first circuit having a heat pump sorbent and a second circuit, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream, a liquid inlet port fluidly connected to the second circuit of the vessel for admitting an aqueous liquid stream or a water stream into the second circuit, and a fluid outlet port fluidly connected to the second circuit of the vessel for recovering the aqueous liquid stream or a steam stream from the second circuit.

15. The system of claim 14, further comprising: a water evaporator or a heat exchanger for converting an aqueous liquid stream comprising water into a stream comprising steam, the water evaporator or the heat exchanger comprising a liquid inlet port fluidly connected to a steam outlet port, a heating inlet port fluidly connected to a heating outlet port, wherein the liquid inlet port is fluidly connected to an aqueous liquid supply, the stream outlet port of the water evaporator or the heat exchanger is fluidly connected to the regeneration port of the sorptive separator, and the fluid outlet port of the vessel is fluidly connected to the heating inlet port of the water evaporator or the heat exchanger.

16. The system of claim 14, wherein the heat pump sorbent in the vessel of the chemical heat pump is configured in the form of a film, a layer, or a sheet, and is interposed between the first circuit and the second circuit of the vessel.

17. The system of any one of claims 14 or 16, wherein the vessel of the chemical heat pump further comprises a diffusion barrier fluidly for separating the first circuit of the vessel and the heat pump sorbent from the second circuit of the vessel and is thermally connected to the heat pump sorbent.

18. The system of any one of claims 14, 16, and 17, wherein the first circuit of the vessel comprises a first circuit volume and the second circuit of the vessel comprises a second circuit volume, wherein the first circuit volume and the second circuit volume are each equal to or less than 30% of a volume in the vessel.

19. The system of any one of claims 14, 16, and 17, wherein the heat pump sorbent is configured in a form of a film, a layer, or a sheet, has a thickness in a range of 0.1 to 1 mm, and a surface area per volume in a range of 250 m²/m³ to 2500 m²/m³.

20. An integrated sorptive gas separation system for separating a first component from a multi-component gas stream, the system comprising:

(a) a sorptive separator further comprising: a sorbent, a feed port for admitting the multi-component gas stream as a feed stream into the sorptive separator, a first product port for recovering a first product stream depleted in the first component relative to the feed stream, a regeneration port for admitting a regeneration stream into the sorptive separator, a second product port for recovering a second product stream enriched in the first component relative to the feed stream, a conditioning port for admitting a conditioning stream into the sorptive separator, and a third product port for recovering a third product stream from the sorptive separator, wherein the feed port is fluidly connected to the first product port, wherein the regeneration port is fluidly connected to the second product port, and wherein the conditioning port is fluidly connected to the third product port; and

(b) a chemical heat pump further comprising: at least one vessel with a first circuit having a heat pump sorbent, a working fluid port fluidly connected to the first circuit of the vessel for admitting a working fluid stream into the vessel, a product port fluidly connected to the first circuit of the vessel for recovering a chemical heat pump product stream, wherein the third product port is fluidly connected to the working fluid port.

21 . The system of claim 20, the system further comprising: a water evaporator or a heat exchanger for converting an aqueous liquid stream comprising water into a stream comprising steam, the water evaporator or the heat exchanger comprising a liquid inlet port fluidly connected to a steam outlet port, a heating inlet port fluidly connected to a heating outlet port, wherein the liquid inlet port is fluidly connected to an aqueous liquid supply, the stream outlet port of the water evaporator or the heat exchanger is fluidly connected to the regeneration port of the sorptive separator, and the fluid outlet port of the vessel is fluidly connected to the heating inlet port of the water evaporator or the heat exchanger.

22. The system of claim 20, wherein the heat pump sorbent in the vessel of the chemical heat pump is configured in the form of a film, a layer, or a sheet, and is interposed between the first circuit and a second circuit of the vessel.

23. The system of claim 22, wherein the vessel of the chemical heat pump further comprises a diffusion barrier for fluidly separating the first circuit of the vessel and the heat pump sorbent from the second circuit of the vessel, and is thermally connected to the heat pump sorbent.

24. The system of claims 22 or 23, wherein the first circuit of the vessel comprises a first circuit volume and the second circuit of the vessel comprises a second circuit volume, wherein the first circuit volume and the second circuit volume are each equal to or less than 30% of a volume in the vessel.

25. The system of any one of claims 20, 23, and 24, wherein the heat pump sorbent is configured in a form of a film, a layer, or a sheet, having a thickness in a range of 0.1 to 1 mm, and a surface area per volume in a range of 250 m²/m³ to 2500 m²/m³.

26. A vessel of a chemical heat pump comprising: a vessel; a heat pump sorbent; a first circuit; and a second circuit, wherein the heat pump sorbent is configured as a film, layer, or sheet, having a thickness in a range of 0.1 and 1 mm, and the heat pump sorbent being interposed between the first circuit and the second circuit, wherein the heat pump sorbent has a surface area per volume in a range of 250m²/m³ and 2500 m²/m³, and wherein the heat pump has a heat capacity equal to or greater than 50% of a heat capacity of the vessel, when the first circuit and second circuit are filled with a gas.