Carbon dioxide capture and conversion integrated system based on crossed flow guide type double parallel pipes

Abstract

The invention belongs to the related field of carbon dioxide capture and conversion technologies, and discloses a carbon dioxide capture and conversion integrated system based on crossed flow guide type double parallel pipes, which comprises the two parallel pipes which are parallel and symmetrical, a sizing communication section for horizontally connecting the two parallel pipes, and other components. According to the bifunctional composite bed layer structure, adsorbent monolithic layers and catalyst monolithic layers are alternately arranged through open pores / closed grids to form a cross flow guide passage, and gas is forced to flow directionally. Wherein in the trapping mode, industrial waste gas penetrates through the catalyst layer and then CO2 is trapped by the adsorption layer; and in the conversion mode, the reducing gas reversely penetrates through the adsorption layer to release CO2 and is converted into a high-added-value product in the catalyst layer. By means of the integrated structural design, the problem of multi-device connection of traditional double reactors connected in parallel is avoided, the system complexity is remarkably reduced, repeated energy consumption can be reduced through cooperation of centralized heating and cross flow guide channel optimization, and the device is particularly suitable for continuous trapping and recycling of industrial waste gas.

Description

Technical Field

[0001] This application belongs to the technical field related to carbon dioxide capture and conversion, and more specifically, relates to an integrated carbon dioxide capture and conversion system based on a cross-flow double parallel tube. Background Art

[0002] The integrated carbon dioxide capture and conversion technology is an integrated technology developed within the framework of carbon capture, utilization and storage technology (CCUS). In this technology, after carbon dioxide is captured from industrial tail gas, it is directly converted into valuable chemical products in situ under the dual functions of an adsorbent and a catalyst without going through the traditional desorption step. In the prior art, some specific schemes for the integrated carbon dioxide capture and conversion have been developed. For example, the oxygen-tolerant nickel-based bifunctional material developed in Patent CN117123229A realizes the efficient capture of CO2 in flue gas and in-situ conversion of methane at a low temperature of 200-350°C, and both the capture rate and the conversion rate are close to 100%; Patent CN117839377A switches the adsorption-catalysis mode through a four-way valve, and can directly heat up and catalyze to produce methane after adsorbing CO2 at room temperature, realizing low-energy consumption continuous operation.

[0003] More specifically, the above prior art mostly adopts a design scheme of two fixed-bed reactors in parallel. For example, in Patents CN114377514A and CN117839377A, the core idea is to achieve continuous production by alternately switching the gas paths of two independent reactors. Such technologies usually fill both reactors with an adsorbent and a catalyst bifunctional material, and use a four-way valve to switch the flow directions of industrial waste gas and hydrogen, so that the capture and conversion modes operate alternately. This kind of design avoids the desorption and regeneration steps of the traditional step-by-step process by simplifying the process, initially verifies the feasibility of integrated continuous production, and partially optimizes the energy consumption in specific scenarios (such as low-concentration CO2 capture). In addition, some patents (such as CN119258710A) further improve the process flexibility by introducing dual-mode switching.

[0004] However, further research shows that the above-mentioned existing solutions still have the following defects or deficiencies: First, due to the parallel structure of the two reactors, synchronous heating of the two independent devices is required, resulting in a significant increase in energy loss. For example, in the traditional solution, high temperatures (200 - 800 °C) need to be applied to the two reactors separately, and the repeated input of heat significantly reduces the energy efficiency of the system. Second, in the above-mentioned existing technology, the mixed loading design of the adsorbent and the catalyst leads to interference between the active sites. Specifically, the volume expansion during the adsorption and desorption process of the adsorbent easily covers the catalytic sites, and the carbon deposition generated during the catalytic reaction clogs the pores of the adsorbent, and the material performance rapidly decays with the number of cycles. Finally, and more critically, in the above-mentioned existing technology, the internal structure of the reactor is not optimized for the gas flow characteristics, and the simple parallel fixed-bed design easily leads to uneven gas flow distribution and too high pressure drop. After scaling up, the mass transfer efficiency is further reduced, making it difficult to meet the industrial-scale high-throughput requirements. Summary of the Invention

[0005] In view of the above defects or improvement requirements of the prior art, the present application provides an integrated carbon dioxide capture and conversion system based on cross-flow double parallel tubes. By redesiging its overall structure composition and making targeted improvements to the specific structure and working mechanism of its key components such as the sizing connection section, it can effectively solve the key problems of redundant energy consumption, interference between active sites, and low mass transfer efficiency caused by uneven gas distribution in the existing parallel design of two reactors, and significantly reduce the system complexity. Therefore, it is particularly suitable for continuous carbon capture and resource utilization applications of carbon-containing industrial waste gas.

[0006] To achieve the above object, the present application provides an integrated carbon dioxide capture and conversion system based on cross-flow double parallel tubes, characterized in that the system includes:

[0007] A double parallel tube unit, which includes two first parallel tubes A and second parallel tubes B that are parallelly arranged and symmetrically structured. A first intake valve is provided at the bottom of the first parallel tube A for controllably connecting to an industrial waste gas source, and a first exhaust valve is provided at its top for controllably discharging the required high-value-added product; a second intake valve is provided at the bottom of the second parallel tube B for controllably connecting to a hydrogen molecule source, and a second exhaust valve is provided at its top for controllably discharging decarbonized waste gas.

[0008] A sizing and connecting section, which is horizontally connected between the first parallel pipe A and the second parallel pipe B, and its inner diameter remains constant along the horizontal axis; the sizing and connecting section sequentially includes a catalyst integrated layer, an adsorbent integrated layer and a heating unit from the inside to the outside, wherein the heating unit is wrapped around the periphery of the sizing and connecting section and is used to provide heat for the capture and conversion of carbon dioxide; the adsorbent integrated layer is arranged on the inner wall of the sizing and connecting section and is used to perform the adsorption and desorption of carbon dioxide; the catalyst integrated layer is integrally in a solid cylindrical shape and is arranged at the central axis part of the sizing and connecting section and is used to perform catalytic reaction on carbon dioxide;

[0009] In addition, the right side of the adsorbent integrated layer horizontally connected to the second parallel pipe B is an open-hole grid, and its left side is a closed grid; the left side of the catalyst integrated layer horizontally connected to the first parallel pipe A is an open-hole grid, and its right side is a closed grid, thereby forming a cross-flow guiding path in this way.

[0010] As a further preference of the present application, the above system has the following working modes:

[0011] Capture mode, in this working mode, industrial waste gas enters from the first intake valve at the bottom of the first parallel pipe A, while keeping the second intake valve and the first exhaust valve closed. The industrial waste gas sequentially penetrates the open-hole grid on the left side of the catalyst integrated layer and the open-hole grid on the right side of the adsorbent integrated layer, and the decarbonized waste gas is discharged from the top of the second parallel pipe B through the second exhaust valve;

[0012] Conversion mode, in this working mode, the reducing gas enters from the second intake valve at the bottom of the second parallel pipe B, while keeping the first intake valve and the second exhaust valve closed. The reducing gas sequentially penetrates the open-hole grid on the right side of the adsorbent integrated layer and the open-hole grid on the left side of the catalytic integrated layer, and the high-value-added product is exported from the top of the first parallel pipe A through the first exhaust valve.

[0013] As a further preference of the present application, for the heating unit, it is preferably heated by an electric heating wire, and is equipped with a temperature sensor and an intelligent temperature control system, and its temperature control accuracy is ±5°C, and the reaction temperature range is 200°C - 800°C.

[0014] As a further preference of the present application, for the adsorbent integrated layer and the catalyst integrated layer, both are preferably in a porous matrix integrated structure, and its configuration is any one of honeycomb, corrugated plate matrix, and foam metal. Among them, the porosity of the adsorbent integrated layer is preferably 30% - 75%, and the porosity of the catalyst integrated layer is preferably 40% - 65%.

[0015] As a further preference of the present application, for the adsorbent monolithic layer, it preferably contains oxides for adsorbing and desorbing carbon dioxide and sulfur-resistant adsorption components, wherein the oxides are at least one of calcium oxide (CaO), magnesium oxide (MgO), barium oxide (BaO), strontium oxide (SrO), and lanthanum oxide (La2O3); the sulfur-resistant adsorption components are transition metal oxides such as Fe2O3, Co3O4, NiO, CuO or MOFs, including any one of metal-organic framework materials such as ZIF-8 and MIL-101, and account for 20%-40% of the total mass of the adsorbent.

[0016] As a further preference of the present application, for the catalyst monolithic layer, it preferably contains a main catalyst and a sulfur-resistant promoter, wherein the main catalyst is at least one metal or its compound among iron (Fe), cobalt (Co), nickel (Ni), ruthenium (Ru), rhodium (Rh), palladium (Pd), indium (In), iridium (Ir), and platinum (Pt), and the sulfur-resistant promoter is a manganese-cerium-cobalt composite oxide (Mn-Ce-Co-O) and rare earth oxides such as Sm2O3 and Eu2O3, and the main catalyst accounts for 60-80 wt%, and the sulfur-resistant promoter accounts for 5-15 wt%.

[0017] As a further preference of the present application, the reducing gas is one of hydrogen (H2), methane (CH4), ethane (C2H6), and methanol (CH3OH).

[0018] As a further preference of the present application, for the adsorbent monolithic layer and the catalyst monolithic layer, the pore shapes of the open-cell gratings of both are preferably regular polygon holes, circular holes, ellipses, stars, crosses, conical holes, and any one or more combinations thereof.

[0019] As a further preference of the present application, the pore diameter of the open-cell grating of the adsorbent monolithic layer is preferably 1.2-1.5 times the diameter of the adsorbent particles in the adsorbent monolithic layer.

[0020] As a further preference, the pore diameter of the open-cell grating of the catalyst monolithic layer is preferably 0.8-1.2 times the pore diameter of the catalyst carrier in the catalyst monolithic layer.

[0021] Generally speaking, compared with the prior art, the above technical solutions conceived by the present application have the following beneficial effects:

[0022] (1) Through the integrated structure of cross-flow double parallel tubes, this application integrates the adsorption and catalytic functions within a compact constant-diameter connection section. By adopting a centralized heating strategy, only precise temperature control of a single functional bed layer is required. The heating unit is wrapped around the periphery of the constant-diameter connection section, and the thermal field distribution is adjusted in real time through an intelligent temperature control system, which can ensure the directional transfer of heat to the active regions of the adsorption layer and the catalytic layer, avoiding heat loss and repeated input in traditional multi-region heating. This design significantly improves the thermal energy utilization efficiency by reducing the thermal inertia load and ineffective heat conduction paths, and is especially suitable for industrial scenarios that require long-term continuous operation, reducing energy consumption and carbon emissions from the source;

[0023] (2) In this application, the adsorption layer and the catalytic layer are designed with physical isolation and layered loading to achieve functional decoupling and independent regeneration. The integrated adsorbent layer is distributed at both ends of the constant-diameter connection section, and the catalytic layer is arranged in the middle. The layout of the open / closed grille ensures that the gas flows in a directional manner according to the preset path, avoiding the physical coverage of the catalytic active surface by the volume expansion during the adsorption and desorption process of the adsorbent. At the same time, the by-products generated by the catalytic reaction are restricted within the independent catalytic layer, preventing them from diffusing into the pores of the adsorption layer and causing blockage. Combining the synergistic effect of sulfur-resistant adsorbent and sulfur-resistant catalyst, the system can still maintain stable capture and conversion efficiency in complex flue gas environments containing sulfur, high humidity, etc., significantly extending the service life of the material;

[0024] (3) In addition, in this application, the cross-flow passage optimizes the gas flow path through the alternating opening and closing design of the porous grille, enhancing the gas-solid contact frequency and the diffusion efficiency of reactants. The high-porosity design of the integrated adsorbent layer effectively reduces the gas passage resistance, and the pore shape and aperture of the flow guide grille are adapted to the size characteristics of the adsorbent particles and the catalyst carrier, ensuring uniform gas distribution. This design effectively realizes the dynamic matching of the adsorption-catalytic process by reconstructing the gas flow path. Brief Description of the Drawings

[0025] Figure 1 is the overall structure diagram of the carbon dioxide capture and conversion integrated system based on the cross-flow double parallel tubes according to this application;

[0026] Figure 2 is the top view of the structure of the carbon dioxide capture and conversion integrated system based on the cross-flow double parallel tubes according to this application;

[0027] Figure 3a is the front view of the structure of the constant-diameter connection section according to the preferred embodiment of this application;

[0028] Figure 3b is the side view of the connection between the constant-diameter connection section and the first parallel tube A according to the preferred embodiment of this application;

[0029] Figure 3cis a side view of the connection between the sizing connecting section and the second parallel pipe B according to a preferred embodiment of the present application;

[0030] Figure 4a is a schematic diagram for exemplarily showing the integrated system of the present application executing a capture mode;

[0031] Figure 4b is a schematic diagram for exemplarily showing the conversion mode executed by the integrated system of the present application;

[0032] In all the drawings, the same reference numerals are used to represent the same structures or elements, wherein:

[0033] 1-first parallel pipe A, 2-second parallel pipe B, 3-diameter connecting section, 4-first air inlet valve, 5-second air inlet valve, 6-first exhaust valve, 7-second exhaust valve, 8-adsorbent monolithic layer, 9-catalyst monolithic layer, 10-heating unit, 11-opening grille, 12-closed grille. DETAILED DESCRIPTION

[0034] In order to make the purpose, technical solution and advantages of the present application more clear, the present application is further described in detail below in conjunction with the embodiments. It should be understood that the specific embodiments described here are only used to explain the present application and are not used to limit the present application.

[0035] It should be understood that expressions such as "include" and "may include" used in this application indicate the existence of the disclosed functions, operations or constituent elements, and do not limit one or more additional functions, operations and constituent elements. In this application, terms such as "include" and / or "have" may be interpreted as indicating specific characteristics, numbers, operations, constituent elements, components or combinations thereof, but may not be interpreted as excluding the existence or possibility of adding one or more other characteristics, numbers, operations, constituent elements, components or combinations thereof.

[0036] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of the features. In the description of this application, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0037] Figure 1 This is the overall structural diagram of the integrated carbon dioxide capture and conversion system based on the cross-flow dual parallel pipes of the present application. Figure 2 This is a top view of the structure of the integrated carbon dioxide capture and conversion system based on the cross-flow dual parallel pipe according to the present application. Figure 1 andFigure 2 To explain the present invention more specifically.

[0038] As Figure 1 and Figure 2 shown in, the integrated carbon dioxide capture and conversion system of the present application mainly includes components such as a double parallel tube unit and a sizing connection section.

[0039] For the double parallel tube unit, the double parallel tube unit includes two first parallel tubes A (denoted by reference numeral 1) and second parallel tubes B (denoted by reference numeral 2) that are arranged in parallel and have a symmetrical structure. A first intake valve 4 is provided at the bottom of the first parallel tube A for controllably connecting to an industrial waste gas source, and a first exhaust valve 6 is provided at the top of the first parallel tube A for controllably discharging the required high-value-added products; a second intake valve 5 is provided at the bottom of the second parallel tube B for controllably connecting to a hydrogen molecule source, and a second exhaust valve 7 is provided at the top of the second parallel tube B for controllably discharging decarbonized waste gas.

[0040] For the sizing connection section, the sizing connection section 3 is horizontally connected between the first parallel tube A and the second parallel tube B, and its inner diameter remains constant along the horizontal axis.

[0041] More specifically, as can be seen in Figures 3a - 3c , the sizing connection section 3 sequentially includes a catalyst integrated layer 9, an adsorbent integrated layer 8, and a heating unit 10 from the inside to the outside. The heating unit 10 is wrapped around the periphery of the sizing connection section 3 and is used to provide heat for the capture and conversion of carbon dioxide; the adsorbent integrated layer 8 is provided on the inner wall of the sizing connection section 3 and is used to perform the adsorption and desorption of carbon dioxide; the catalyst integrated layer 9 is integrally in a solid cylindrical shape and is provided at the central axis position of the sizing connection section 3 and is used to perform a catalytic reaction on carbon dioxide.

[0042] In addition, the right side of the adsorbent integrated layer 8 that is horizontally connected to the second parallel tube B is an open grid, and its left side is a closed grid; the left side of the catalyst integrated layer 9 that is horizontally connected to the first parallel tube A is an open grid, and its right side is a closed grid, thereby forming a cross-flow type passage in this way.

[0043] The working principle of the integrated system according to the present application will be specifically described below.

[0044] As can be seen in Figure 4a and 4b , the above system has the following working modes:

[0045] Capture mode: In this working mode, industrial waste gas enters from the first air inlet valve 4 at the bottom of the first parallel pipe A, while keeping the second air inlet valve 5 and the first exhaust valve 6 in a closed state, and the industrial waste gas sequentially penetrates the open grid on the left side of the catalyst monolithic layer 9 and the open grid on the right side of the adsorbent monolithic layer 8, and the decarbonized waste gas is discharged from the top of the second parallel pipe B through the second exhaust valve 7;

[0046] Conversion mode: In this working mode, reducing gas enters from the second intake valve 5 at the bottom of the second parallel pipe B, while keeping the first intake valve 4 and the second exhaust valve 7 in a closed state, and the reducing gas sequentially penetrates the open grille on the right side of the adsorbent monolith 8 and the open grille on the left side of the catalytic monolith 9, and the high value-added product is discharged from the top of the first parallel pipe A1 through the first exhaust valve 6. In this process, the carbon deposits generated by the catalytic reaction are confined in the catalytic layer and removed by periodic regeneration to avoid clogging the adsorbent pores.

[0047] According to a preferred embodiment of the present application, the heating unit 10 preferably adopts electric heating wire heating, and is equipped with a temperature sensor and an intelligent temperature control system, with a temperature control accuracy of ±5°C and a reaction temperature range of 200°C-800°C.

[0048] According to a preferred embodiment of the present application, the adsorbent monolith 8 adopts an anti-sulfur composite adsorbent to preferentially adsorb sulfides in the flue gas; the catalyst monolith 9 contains an anti-sulfur additive, thereby maintaining catalytic activity in a sulfur-containing environment.

[0049] Through the above conception, the cross-flow path optimizes the gas flow path through the above layout design of the open grid 11 and the closed grid 12, forces the gas flow to form turbulence, enhances the gas-solid contact efficiency, and reduces the bed pressure drop. At the same time, the above integrated system controls the alternating operation of the capture and conversion modes through valve switching, adjusts the switching cycle in real time according to the adsorbent saturation, and reduces ineffective energy consumption.

[0050] According to another preferred embodiment of the present application, for the adsorbent monolithic layer 8 and the catalyst monolithic layer 9, both are preferably porous matrix monolithic structures, and their configurations are any one of honeycomb, corrugated plate matrix, and foam metal, wherein the porosity of the adsorbent monolithic layer 8 is preferably 30%-75%, and the porosity of the catalyst monolithic layer 9 is preferably 40%-65%.

[0051] According to another preferred embodiment of the present application, for the adsorbent monolithic layer 8, it preferably contains oxides for adsorbing and desorbing carbon dioxide and sulfur-resistant adsorption components, wherein the oxides are at least one of calcium oxide (CaO), magnesium oxide (MgO), barium oxide (BaO), strontium oxide (SrO), and lanthanum oxide (La2O3); the sulfur-resistant adsorption components are transition metal oxides such as Fe2O3, Co3O4, NiO, CuO, or MOFs, including any one of metal-organic framework materials such as ZIF-8 and MIL-101, and account for 20%-40% of the total mass of the adsorbent. For the catalyst monolithic layer 9, it preferably contains a main catalyst and a sulfur-resistant promoter, wherein the main catalyst is at least one metal or its compound among iron (Fe), cobalt (Co), nickel (Ni), ruthenium (Ru), rhodium (Rh), palladium (Pd), indium (In), iridium (Ir), and platinum (Pt), and the sulfur-resistant promoter is a manganese-cerium-cobalt composite oxide (Mn-Ce-Co-O) and rare earth oxides such as Sm2O3 and Eu2O3, and the main catalyst accounts for 60-80 wt%, and the sulfur-resistant promoter accounts for 5-15 wt%.

[0052] According to another preferred embodiment of the present application, for the adsorbent monolithic layer 8 and the catalyst monolithic layer 9, the pore shapes of the open-cell gratings of both are preferably regular polygon holes, circular holes, ellipses, stars, crosses, conical holes, or any combination of the above. More specifically, the pore diameter of the open-cell grating of the adsorbent monolithic layer 8 is preferably 1.2-1.5 times the diameter of its adsorbent particles, and the pore diameter of the open-cell grating of the catalyst monolithic layer 9 is preferably 0.8-1.2 times the pore diameter of its catalyst carrier.

[0053] In summary, compared with the prior art, the present application makes full use of the alternating layout of open / closed gratings to form a directional flow passage, forcing the gas to flow along a preset path; the heating device is wrapped around the fixed-diameter connection section to centrally heat the dual-functional composite bed layer, providing stable heat for the adsorption and catalytic reactions; through the switching control of the intake valve and the exhaust valve, the manual alternating operation of the capture mode and the conversion mode is realized. The physical isolation design of the adsorption layer and the catalytic layer avoids interference with the material properties, and the synergistic effect of the sulfur-resistant adsorbent and the catalyst is adapted to the sulfur-containing flue gas environment. The present invention has the advantages of compact structure, low energy consumption, and flexible operation, and is suitable for the continuous carbon capture and resource utilization requirements in high-carbon emission industrial scenarios such as steel and chemical industries, especially for the treatment of sulfur-containing and high-dust complex flue gases, and thus has good practical value and application prospects.

[0054] It is easy for those skilled in the art to understand that the above are only preferred embodiments of the present application and are not intended to limit the present application. Any modifications, equivalent replacements, and improvements made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A carbon dioxide capture and conversion integrated system based on cross-flow double parallel pipes, characterized in that: The system includes: A double parallel pipe unit, the double parallel pipe unit comprising two parallel and symmetrically arranged first parallel pipes A (1) and second parallel pipes B (2), wherein the bottom of the first parallel pipe A (1) is provided with a first air intake valve (4) for controllably connecting to an industrial waste gas source, and the top of the first parallel pipe A (1) is provided with a first air exhaust valve (6) for controllably discharging the required high value-added products; the bottom of the second parallel pipe B (2) is provided with a second air intake valve (5) for controllably connecting to a hydrogen molecule source, and the top of the second parallel pipe B (2) is provided with a second air exhaust valve (7) for controllably discharging decarbonized waste gas; A sizing connecting section, wherein the sizing connecting section (3) is horizontally connected between the first parallel pipe A (1) and the second parallel pipe B (2), and its inner diameter is kept constant along the horizontal axis; the sizing connecting section (3) comprises, from the inside to the outside, a catalyst monolithic layer (9), an adsorbent monolithic layer (8) and a heating unit (10), wherein the heating unit (10) is wrapped around the periphery of the sizing connecting section (3) and is used to provide heat for the capture and conversion of carbon dioxide; the adsorbent monolithic layer (8) is arranged on the inner wall of the sizing connecting section (3) and is used to perform the adsorption and desorption of carbon dioxide; the catalyst monolithic layer (9) is in the shape of a solid cylinder as a whole and is arranged at the central axis of the sizing connecting section (3) and is used to perform a catalytic reaction on carbon dioxide; In addition, the right side of the adsorbent monolithic layer (8) horizontally connected to the second parallel tube B (2) is an open-hole grille, and the left side thereof is a closed grille; the left side of the catalyst monolithic layer (9) horizontally connected to the first parallel tube A (1) is an open-hole grille, and the right side thereof is a closed grille, thereby forming a cross-flow-guiding passage.

2. The integrated carbon dioxide capture and conversion system according to claim 1, characterized in that: The above system has the following working modes: Capture mode, in this working mode, industrial waste gas enters from the first air inlet valve (4) at the bottom of the first parallel pipe A (1), while the second air inlet valve (5) and the first exhaust valve (6) are kept in a closed state, and the industrial waste gas sequentially penetrates the open grille on the left side of the catalyst monolithic layer (9) and the open grille on the right side of the adsorbent monolithic layer (8), and the decarbonized waste gas is discharged from the top of the second parallel pipe B (2) through the second exhaust valve (7); Conversion mode. In this working mode, reducing gas enters from the second air inlet valve (5) at the bottom of the second parallel pipe B (2). At this time, the first air inlet valve (4) and the second air exhaust valve (7) are kept in a closed state. The reducing gas sequentially penetrates the perforated grille on the right side of the adsorbent monolithic layer (8) and the perforated grille on the left side of the catalytic monolithic layer (9). High value-added products are discharged from the top of the first parallel pipe A (1) through the first exhaust valve (6).

3. The integrated carbon dioxide capture and conversion system according to claim 1 or 2, characterized in that: As for the heating unit (10), it is preferably heated by an electric heating wire and is equipped with a temperature sensor and an intelligent temperature control system. The temperature control accuracy is ±5°C and the reaction temperature range is 200°C-1000°C.

4. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 3, characterized in that: As for the adsorbent monolithic layer (8) and the catalyst monolithic layer (9), both are preferably porous matrix monolithic structures, and their configuration is any one of honeycomb, corrugated plate matrix, and foam metal, wherein the porosity of the adsorbent monolithic layer (8) is preferably 30%-75%, and the porosity of the catalyst monolithic layer (9) is preferably 40%-65%.

5. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 4, characterized in that: For the adsorbent monolithic layer (8), it preferably comprises an oxide for absorbing and desorbing carbon dioxide and an anti-sulfur adsorption component, wherein the oxide is at least one of calcium oxide (CaO), magnesium oxide (MgO), barium oxide (BaO), strontium oxide (SrO) and lanthanum oxide (La2O3); the anti-sulfur adsorption component is transition metal oxides such as Fe2O3, Co3O4, NiO, CuO or MOFs, including any one of metal organic framework materials such as ZIF-8 and MIL-101, and accounts for 20%-40% of the total mass of the adsorbent.

6. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 5, characterized in that: For the catalyst package layer (9), it preferably comprises a main catalyst and an anti-sulfur additive, wherein the main catalyst is at least one metal or its compound selected from the group consisting of iron (Fe), cobalt (Co), nickel (Ni), ruthenium (Ru), rhodium (Rh), palladium (Pd), indium (In), iridium (Ir), and platinum (Pt), and the anti-sulfur additive is manganese-cerium-cobalt composite oxide (Mn-Ce-Co-O) and rare earth oxides such as Sm2O3 and Eu2O3, and the main catalyst accounts for 60-80wt%, and the anti-sulfur additive accounts for 5-15wt%.

7. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 6, characterized in that: The reducing gas is one of hydrogen (H2), methane (CH4), ethane (C2H6), and methanol (CH3OH).

8. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 7, characterized in that: For the adsorbent monolithic layer (8) and the catalyst monolithic layer (9), the hole shapes of the perforated grids of both are preferably regular polygonal holes, circular holes, ellipses, stars, crosses, conical holes, and any one or more combinations thereof.

9. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 8, characterized in that: The pore size of the open grid of the adsorbent monolithic layer (8) is preferably 1.2-1.5 times the diameter of the adsorbent particles in the adsorbent monolithic layer (8); the pore size of the open grid of the catalyst monolithic layer (9) is preferably 0.8-1.2 times the pore size of the catalyst carrier in the catalyst monolithic layer (9).

10. The integrated carbon dioxide capture and conversion system according to any one of claims 1 to 9, characterized in that: The system is not only suitable for carbon dioxide capture and conversion, but can also be widely used to treat other types of industrial waste gases, including but not limited to the capture and conversion of harmful gases such as nitrogen oxides (NOx), sulfides (SOx), volatile organic compounds (VOCs), ammonia (NH3), and methane (CH4). It can also convert these waste gases into harmless gases or high value-added products through different adsorbent and catalyst combinations.

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