In-situ carbon capture and conversion method based on three-way catalyst

Abstract

The invention relates to the technical field of catalysts, in particular to an in-situ carbon capture and conversion method based on a three-way catalyst. The invention provides a design idea of in-situ state carbon capture and carbon conversion, and is realized by designing a three-way catalyst, and the three-way catalyst comprises an active component A for catalyzing organic matter steam reforming reaction, an active component B for catalyzing CO2 in-situ conversion reaction and a carrier with CO2 capture performance; the active component A is at least one of Ni, Co, Fe, Mn, Pt, Ru, Rh and Pd; the active component B is at least one of Ni, Fe, Co, Mo, Pt, Ru, Rh, Pd, Cu, Zn and Al. The method has multiple functions of catalyzing reforming of organic matter steam to produce hydrogen, and realizing in-situ capture and in-situ conversion of carbon dioxide to generate high-value organic fuel.

Description

Technical Field

[0001] The present invention relates to the field of catalyst technology, and in particular to an in-situ carbon capture and conversion method based on a three-way catalyst. Background Art

[0002] The steam reforming reaction of organic matter is a process in which hydrocarbons (or hydrocarbon hydroxides) and water vapor react at high temperatures to produce CO2 and H2. Among them, the most typical reaction is the methane steam reforming reaction. At present, more than 80% of the world's hydrogen is produced by reforming compounds containing carbon and hydrogen elements, and the optimization and improvement of the energy efficiency of the reaction is of great significance.

[0003] By capturing CO2 in situ at the reaction equilibrium state, the reaction equilibrium can be moved forward, the reaction conversion rate can be increased, the reaction temperature can be reduced, and the reaction heat loss can be reduced, thereby improving the energy utilization efficiency and hydrogen production efficiency. After absorbing / adsorbing CO2, traditional CO2 capture materials usually require a regeneration process for the capture material, which is generally carried out by inert gas purging and vacuuming. Among them, the inert gas purge requires, on the one hand, to increase the temperature of the inert gas to the reaction temperature, or to reduce the temperature of the capture material to room temperature, both of which require a temperature rise and temperature drop cycle, in which a large amount of heat is difficult to be efficiently recovered, especially the low solid heat recovery efficiency restricts the improvement of carbon capture efficiency. By reducing the partial pressure by vacuuming, the mechanical efficiency of the vacuum pump decreases exponentially with the reduction of the separation pressure. When the vacuum pressure is reduced to below 0.01 bar, the mechanical efficiency will be less than 1%, so the separation energy consumption increases sharply, which also seriously limits the energy utilization efficiency of the carbon capture process.

[0004] In summary, low energy efficiency limits the large-scale application and promotion of carbon capture, but there is currently no technical solution to efficiently achieve carbon capture. Summary of the invention

[0005] Based on the above content, the present invention provides an in-situ carbon capture and conversion method based on a three-way catalyst. The method proposed in the present invention can not only efficiently catalyze the reforming reaction of organic compounds containing carbon and hydrogen with water vapor, but also efficiently capture the CO2 generated by the reaction and convert it under specific conditions, such as in-situ CO2 hydrogenation or methane reforming reaction, so that the adsorbed / absorbed CO2 is directly converted into high-value products, avoiding the high-energy consumption CO2 capture material regeneration process, and improving the overall reaction efficiency.

[0006] To achieve the above object, the present invention provides the following solutions:

[0007] One of the technical solutions of the present invention is a three-way catalyst for in-situ carbon capture and conversion, comprising an active component A for catalyzing the steam reforming reaction of organic matter, an active component B for catalyzing the in-situ conversion reaction of CO2, and a carrier with CO2 capture performance;

[0008] The active component A is at least one of Ni, Co, Fe, Mn, Pt, Ru, Rh, and Pd;

[0009] The active component B is at least one of Ni, Fe, Co, Mo, Pt, Ru, Rh, Pd, Cu, Zn, and Al;

[0010] The carrier is at least one of CaO, MgO, Ca(OH)2, Mg(OH)2, Li2ZrO3, Li2SiO3, Li4SiO4, zeolite, hydrotalcite or molecular sieve.

[0011] The present invention considers adding a CO2 in-situ conversion reaction on the basis of the traditional organic steam reforming hydrogen production reaction, and combines the two reactions by creatively designing a three-effect catalyst.

[0012] In some preferred embodiments of the present invention, the mass ratio of the active component A to the active component B is 1:(0.1-10), and the mass ratio of the active component A to the carrier is 1:(1-10000).

[0013] Furthermore, the mass ratio of the active component A to the active component B is 1:(0.1-5), and the mass ratio of the active component A to the carrier is 1:(1-1000).

[0014] In some preferred embodiments of the present invention, the specific surface area of ​​the carrier is 1-500m 2 / g.

[0015] In some preferred embodiments of the present invention, the particle sizes of the active component A and the active component B are independently 10-10000 nm.

[0016] In some preferred embodiments of the present invention, the carrier is a CaO-MgO carrier or a Li2ZrO3-Al2O3 carrier;

[0017] The CaO-MgO carrier is prepared by mixing CaO powder and MgO powder in a mass ratio of 12:4.8, adding a small amount of deionized water, stirring evenly to form a slurry, and then drying at 100° C. for 12 hours.

[0018] The Li2ZrO3-Al2O3 carrier is prepared by mixing Li2ZrO3 powder and Al2O3 powder in a mass ratio of 3:1, adding a small amount of deionized water and stirring evenly to form a slurry, and then drying at 130° C. for 18 hours.

[0019] Compared with single-component carriers, composite carriers can improve the thermal stability of carriers and enhance redox ability. Taking CaO-MgO carriers and Li2ZrO3-Al2O3 carriers as examples, carriers prepared using the above raw material ratio parameters, drying temperature and time have a longer service life than carriers prepared using other raw material ratio parameters, drying temperature and time while maintaining high CO2 absorption.

[0020] The second technical solution of the present invention is a method for preparing the above-mentioned three-way catalyst for in-situ carbon capture and conversion, which is prepared by compounding active component A, active component B and a carrier. The compounding method can adopt a common preparation method in the art, such as a gas phase method, a liquid phase method, a solid phase method, a plasma method, etc. The three-way catalyst synthesis method only needs to meet the following requirements, and a suitable synthesis method can be selected according to actual conditions:

[0021] (1) Selecting the corresponding active component A, active component B and carrier component according to the reaction required for production;

[0022] (2) Rationally design the molar mass ratio of active component A, active component B and carrier component in the three-way catalyst based on the catalytic effect;

[0023] (3) According to the designed ratio, select a suitable preparation method to achieve the working conditions required for synthesis, and combine the three different components (active component A, active component B and carrier component) into the desired target product.

[0024] For example, when the liquid phase method is used, the preparation method of the three-way catalyst for in-situ carbon capture and conversion comprises the following steps:

[0025] Dissolving a salt containing active component A in water to obtain an active component A solution;

[0026] Dissolving a salt containing active component B in water to obtain an active component B solution;

[0027] The active component A solution, the active component B solution and the carrier are uniformly mixed according to the mass ratio of active component A to active component B and the carrier, and then dried and calcined to obtain the three-way catalyst for in-situ carbon capture and conversion.

[0028] The drying temperature is 100-200° C. and the drying time is 2-18 hours.

[0029] The calcination temperature is 500-1000° C. and the calcination time is 4-12 hours.

[0030] In the present invention, the purpose of drying is to evaporate the water. If the drying step is omitted and calcination is performed directly, the catalyst structure will change due to excessive water, thereby affecting the catalytic performance.

[0031] A third technical solution of the present invention is the use of the above-mentioned three-way catalyst for in-situ carbon capture and conversion in catalyzing steam reforming reactions of organic matter and / or catalyzing in-situ conversion reactions of CO2.

[0032] The third technical solution of the present invention is an in-situ carbon capture and conversion method based on the above-mentioned three-way catalyst, wherein the three-way catalyst is used to catalyze the steam reforming reaction of organic matter. When the concentration of CO2 in the product remains unchanged, it means that the catalyst has absorbed CO2 close to the saturation state, and the organic steam reforming reaction is basically completed, which means that CO2 has accumulated to be sufficient to support the next step of the CO2 in-situ conversion reaction. At this time, the organic steam reforming reaction is stopped, and the three-way catalyst is switched to catalyze the CO2 in-situ conversion reaction. In the catalytic CO2 in-situ conversion reaction, when the concentration of the target product (such as methane, ethane and / or ethylene gas) does not change, it means that the CO2 in-situ conversion reaction is basically completed, and the three-way catalyst is switched to catalyze the organic steam reforming reaction, and the above-mentioned catalytic organic steam reforming reaction and catalytic CO2 in-situ conversion reaction operations are repeated.

[0033] In some preferred embodiments of the present invention, in the organic matter steam reforming reaction, the molar ratio of steam to hydrocarbon is (1-10):1, and the space velocity is 1-360000m 3 h -1 , the reaction temperature is 100-1000℃, and the reaction pressure range is 1-30bar;

[0034] The temperature of the catalytic CO2 in-situ conversion reaction is 100-1000°C, and the reaction pressure ranges from 1-30 bar.

[0035] In some preferred embodiments of the present invention, the catalytic CO2 in-situ conversion reaction includes a CO2 hydrogenation reaction and a CO2 dry reforming reaction.

[0036] The present invention discloses the following technical effects:

[0037] Compared with traditional catalytic methods, the method proposed in the present invention has many advantages: 1) improve the energy efficiency of steam reforming reaction of organic matter, reduce reaction temperature, reduce heat energy loss, and improve energy utilization efficiency; 2) save energy consumption of carbon capture material regeneration: by converting the captured CO2 into high-value-added organic fuel in situ, avoid the high-energy consumption of CO2 capture material regeneration process, and save energy consumption of carbon capture cycle. The conversion process can include hydrogenation reaction and dry reforming reaction; 3) The system is highly integrated and compact: the catalyst can realize organic steam reforming reaction, CO2 capture, and CO2 in-situ conversion reaction, integrating the three traditional system units into one, saving reaction space. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0039] Figure 1 A microscopic schematic diagram of the three-way catalyst designed for the present invention.

[0040] Figure 2 The present invention provides a schematic diagram of the reaction process for the design idea.

[0041] In the figure, 1-active component A catalyzing the hydrogen production reaction of low-value organic matter water vapor; 2-active component B catalyzing the in-situ conversion reaction of CO2; 3-carrier with CO2 adsorption and analysis performance. DETAILED DESCRIPTION

[0042] Various exemplary embodiments of the present invention will now be described in detail. This detailed description should not be considered as limiting the present invention, but should be understood as a more detailed description of certain aspects, features, and embodiments of the present invention.

[0043] It should be understood that the terms described in the present invention are only for describing a particular embodiment and are not intended to limit the present invention. In addition, for the numerical range in the present invention, it should be understood that each intermediate value between the upper and lower limits of the scope is also specifically disclosed. The intermediate value in any stated value or stated range, and each smaller range between any other stated value or intermediate value in the described range is also included in the present invention. The upper and lower limits of these smaller ranges can be independently included or excluded in the scope.

[0044] Unless otherwise indicated, all technical and scientific terms used herein have the same meanings as those generally understood by those skilled in the art. Although the present invention describes only preferred methods and materials, any methods and materials similar or equivalent to those described herein may also be used in the implementation or testing of the present invention. All documents mentioned in this specification are incorporated by reference to disclose and describe the methods and / or materials associated with the documents. In the event of a conflict with any incorporated document, the content of this specification shall prevail.

[0045] It will be apparent to those skilled in the art that various modifications and variations may be made to the specific embodiments of the present invention description without departing from the scope or spirit of the present invention. Other embodiments derived from the present invention description will be apparent to the skilled artisan. The present invention description and examples are exemplary only.

[0046] The words “include,” “including,” “have,” “contain,” etc. used in this document are open-ended terms, meaning including but not limited to.

[0047] The present invention provides a method for in-situ carbon capture and conversion based on a three-way catalyst, which includes multiple functions of an organic matter steam reforming reaction process, a CO2 in-situ capture reaction, and a CO2 in-situ conversion reaction (such as a hydrogenation reaction and a dry reforming reaction) to generate organic fuel. The three-way catalyst of the present invention can reduce process energy consumption and improve the energy utilization efficiency of the reforming reaction and the carbon capture process.

[0048] The working process of the in-situ carbon capture and conversion method based on a three-way catalyst of the present invention includes three parts:

[0049] 1) Organic steam reforming reaction: Taking organic steam reforming as an example, most organic matter and water vapor undergo reforming reaction under high temperature conditions (100-1000℃) and the action of catalyst to generate CO, CO2 and H2. The chemical reaction formula of this process is:

[0050] C x H y O Z +H2O→CO+H2+CO2

[0051] 2) CO2 capture: organic steam reforming reaction (C x H y O Z +H2O→CO+H2+CO2), the gas component contains a certain amount of CO2, which is adsorbed / absorbed by the capture material (such as CaO, MgO, etc.) in the catalyst, so that the reforming reaction equilibrium moves forward, improves the reaction conversion rate and reduces the reaction temperature. As the CO2 concentration in the product (CO+H2+CO2) decreases, the CO and H2O in the product will further generate CO2 and H2 through the water vapor shift reaction, and finally the product will be converted into H2 and captured CO2. Taking CaO as an example, the chemical reaction formula of this process is:

[0052] CO+H2O→CO2+H2

[0053] CO2+CaO→CaCO3

[0054] 3) In-situ CO2 conversion reaction: The catalyst after capturing CO2 is converted into high-value products in-situ and the carbon capture material is regenerated, which can be achieved through in-situ hydrogenation and dry reforming reactions. Taking the hydrogenation reaction with CaO as the carbon capture material and methane as the product as an example, the chemical reaction formula of this process is:

[0055] CaCO3+4H2→CH4+2H2O+CaO

[0056] Taking the dry reforming reaction with CaO as the carbon capture material and methane as the reactant as an example, the chemical reaction formula of this process is:

[0057] CaCO3+CH4→2CO+2H2+CaO

[0058] Through the above process, the three-way catalyst of the present invention realizes efficient hydrocarbon steam reforming, CO2 capture and in-situ conversion, thereby achieving the purpose of reducing energy consumption and improving carbon capture energy efficiency.

[0059] The microscopic schematic diagram of the three-way catalyst of the present invention is as follows Figure 1 As shown; the reaction flow diagram of the three-way catalyst of the present invention is as shown Figure 2 In the figure, 1-active component A catalyzing the steam reforming reaction of organic matter; 2-active component B catalyzing the in-situ conversion reaction of CO2; 3-carrier with CO2 capture performance.

[0060] The technical solutions described in the present invention, unless otherwise specified, are all conventional solutions in the art, and the reagents or raw materials used, unless otherwise specified, are purchased from commercial channels or have been disclosed.

[0061] The technical solutions provided by the present invention are described in detail below in conjunction with the embodiments, but they should not be construed as limiting the protection scope of the present invention.

[0062] Example 1: Preparation of a three-way catalyst (Ni-Cu CaMgO2) with Ni and Cu as active components

[0063] Prepare active component A solution: weigh 5 g Ni(NO3)2·6H2O and dissolve it in 100 mL deionized water to obtain Ni(NO3)2 solution.

[0064] Prepare active component B solution: weigh 5 g Cu(NO3)2·3H2O and dissolve it in 100 mL deionized water to obtain Cu(NO3)2 solution.

[0065] Preparation of carrier C material: 25 g of CaO powder and 25 g of MgO powder were weighed and mixed, a small amount of deionized water was added and stirred evenly to make a slurry, and dried at 100° C. for 12 hours to obtain a CaO-MgO carrier material.

[0066] Preparation of a three-way catalyst: According to the mass ratio of Ni:Cu:CaO-MgO carrier material of 1:1:10, the active component A solution, the active component B solution and the carrier C material are uniformly mixed, dried at 100°C for 12 hours, and then calcined at 500°C for 4 hours to obtain a three-way catalyst (the particle size of Ni in the three-way catalyst is 10-100 nm, and the particle size of Cu is 5-50 nm).

[0067] The mechanism of action of the three-way catalyst prepared in this embodiment is as follows:

[0068] In the catalytic methane steam reforming reaction, the Ni active component catalyzes the reaction of methane and steam at high temperature to generate synthesis gas. The Ni surface provides reactive sites to promote the decomposition of CH4 and its reaction with H2O. The reaction that occurs at this time is:

[0069] CH4+2H2O→CO2+4H2

[0070] The CO2 generated by the reforming reaction is adsorbed by the CaO-MgO carrier material at the reaction temperature. Due to the high specific surface area and adsorption performance of CaO-MgO, CO2 can be effectively captured. Under the catalytic action of the Ni active component, the captured CO2 is methanated with H2 to generate high-value products. The mechanism is that the Ni surface provides active sites, and Cu acts as a co-catalyst to jointly promote the reaction of CO2 and H2:

[0071] CO2+4H2→CH4+2H2O

[0072] Example 2: Preparation of a three-way catalyst (Ni / CuO-ZnO-Al2O3 / CaO-Al2O3) with CuZnAl as active component

[0073] Prepare active component A solution: weigh 0.05 mol Cu(NO3)2 and dissolve it in 50 mL deionized water to obtain a Cu(NO3)2 solution.

[0074] Prepare the active component B solution: weigh 0.05 mol Zn(NO3)2 and dissolve it in 50 mL deionized water to obtain a Zn(NO3)2 solution.

[0075] Prepare the active component C solution: weigh 0.05 mol Al(NO3)3 and dissolve it in 50 mL of deionized water to obtain an Al(NO3)3 solution.

[0076] Prepare the active component D solution: weigh 0.01 mol Ni(NO3)2 and dissolve it in 50 mL of deionized water to obtain a Ni(NO3)2 solution.

[0077] Preparation of carrier E material: 10 g of CaO powder was weighed and mixed with 2 g of porous Al2O3 powder, and a small amount of deionized water was added and stirred evenly to make a slurry, which was dried at 130°C for 18 hours to obtain a CaO-Al2O3 carrier material.

[0078] Preparation of a three-way catalyst: evenly mix the above solution A, solution B, solution C, solution D, and material E, add citric acid to adjust the pH of the reaction system to 5, dry at 100°C for 12 hours, and then calcine at 500°C for 6 hours to obtain a three-way catalyst (the particle size of the CuZnAl metal oxide in the three-way catalyst is about 10-100 nm, and the particle size of the Ni oxide is about 5-50 nm).

[0079] The mechanism of action of the three-way catalyst prepared in this embodiment is as follows:

[0080] Catalytic methane steam reforming reaction: Ni active components catalyze the reaction of methane and water vapor at high temperatures. The mechanism is that the Ni surface provides reactive sites, promoting the decomposition of CH4 and its reaction with H2O.

[0081] CH4+2H2O→CO2+4H2

[0082] The CO2 generated by the reforming reaction is adsorbed by the CaO carrier material at the reaction temperature. Due to the high specific surface area and adsorption performance of porous Al2O3, CO2 can be effectively captured.

[0083] The captured CO2 reacts with H2 to produce methanol under the catalytic action of the surface active sites of the CuZnAl active component.

[0084] CO2+3H2→CH3OH+H2O

[0085] Effect Example 1

[0086] 20 g of the catalyst prepared in the above example and the carrier CaO-Al2O3 without active components were taken as benchmarks for comparison, and the performance of the catalyst was tested using the following method.

[0087] The test process was carried out in two fixed bed reactors, the catalyst dosage was 10g, the organic (methane) steam reforming reaction temperature was 550℃, the steam reforming reactor was carried out, the molar ratio of water vapor to methane was 3:1, and the gas flow rate was 200mL / min. The reaction that occurred was CH4+2H2O→CO2+4H2. The catalytic CO2 in-situ conversion reaction was carried out in the hydrogenation reactor, the reaction temperature was 300℃, the pressure was 10bar, and the reaction that occurred was CO2+3H2→CH3OH+H2O. During the reaction process, the catalyst circulated repeatedly in the two reactors, the residence time in the steam reforming reactor was 10h, and the residence time in the hydrogenation reactor was 30min. After the organic steam reforming reaction was carried out for 1 hour and 10 hours, the reaction products were analyzed by gas phase mass spectrometer, the real-time concentrations of gases such as H2, CO2 and CH4 were monitored, and recorded, and the results are statistically shown in Table 1. After the hydrogenation reactor reacted for 30 minutes, the reaction product was analyzed by gas mass spectrometry, and the statistical results are shown in Table 2.

[0088] Table 1. Results of steam reforming of methane catalyzed by three-way catalysts

[0089]

[0090] Note: "-" in the table means that the target product was not detected in this group of experiments, that is, no target product was generated or the concentration of the target product was lower than the lower limit of instrument detection accuracy (0.01%).

[0091] Effect Example 2

[0092] The only difference from effect example 1 is that the catalytic CO2 in-situ conversion reaction is carried out in a hydrogenation reactor, the reaction temperature is 400°C, the pressure is 1 bar, and the reaction that occurs is CO2+4H2→CH4+2H2O. The results are summarized in Table 2.

[0093] Effect Example 3

[0094] The only difference from effect example 1 is that the catalytic CO2 in-situ conversion reaction is carried out in a hydrogenation reactor, the reaction temperature is 800°C, the pressure is 10 bar, and the reactions that occur are 2CO2+7H2→C2H6+4H2O, 2CO2+6H2→C2H4+4H2O, and 3CO2+10H2→C3H8+6H2O. The results are summarized in Table 2.

[0095] Effect Example 4

[0096] The only difference from effect example 1 is that the catalytic CO2 in-situ conversion reaction is carried out in a hydrogenation reactor, the reaction temperature is 250°C, the pressure is 1 bar, and the reaction that occurs is CO2+H2→CO+H2O. The results are summarized in Table 2.

[0097] Table 2. Gas data of three-way catalyst saturated with CO2 and then hydrogenated at 650℃ for 2h

[0098]

[0099] As can be seen from Table 1, in the steam methane reforming reaction, the three-way catalyst prepared by the preparation method of the three-way catalyst provided by the present invention has a methane conversion rate, a hydrogen yield, and a carbon dioxide absorption rate at different time periods of the catalysts of Example 1 and Example 2 that are higher than the benchmark catalyst CaO-Al2O3. It shows that the three-way catalyst of the present invention can effectively produce hydrogen and improve the methane yield in the methane steam reforming reaction. Compared with the steam methane reforming catalyst of the traditional industry, the three-way catalyst of the present invention not only has higher activity and stability, but also can promote the reaction and improve the selectivity of the reaction.

[0100] From the analysis of Table 2, it can be seen that the three-way catalyst of the present invention can convert carbon dioxide in situ to increase the yield of organic matter, avoid the high energy consumption of CO2 capture material regeneration process, convert carbon dioxide into high-value products, improve energy utilization, and reduce energy consumption in the reaction.

[0101] The present invention prepares an in-situ carbon capture and conversion method based on a three-way catalyst by compositely preparing an active component that catalyzes the steam reforming reaction of organic matter, an active component that catalyzes the in-situ conversion reaction of CO2, and a carrier with CO2 capture performance. The method can avoid the high-energy consumption CO2 capture material regeneration process, convert carbon dioxide into high-value products, reduce the reaction temperature and reaction heat loss, improve energy utilization efficiency and hydrogen production efficiency, and achieve the technical effect of 1+1+1 greater than 3.

[0102] It should be noted that the catalytic CO2 in-situ conversion reaction in the present invention does not require desorption of CO2 in the catalyst. In the catalytic CO2 in-situ conversion reaction, the CO2 in the catalyst is allowed to participate in the reaction by hydrogenation or the introduction of methane. As the carbon dioxide hydrogenation reaction or the methane dry reforming reaction proceeds, the carbon dioxide captured in the catalyst is consumed, that is, the catalytic CO2 in-situ conversion reaction process is the regeneration process of the carbon dioxide capture material (such as adsorbent, absorbent).

[0103] The embodiments described above are only descriptions of the preferred modes of the present invention, and are not intended to limit the scope of the present invention. Without departing from the design spirit of the present invention, various modifications and improvements made to the technical solutions of the present invention by ordinary technicians in this field should all fall within the protection scope determined by the claims of the present invention.

Claims

1. A three-way catalyst for in-situ carbon capture and conversion, characterized in that: It comprises an active component A for catalyzing steam reforming reaction of organic matter, an active component B for catalyzing in-situ conversion reaction of CO2, and a carrier with CO2 capture performance; The active component A is at least one of Ni, Co, Fe, Mn, Pt, Ru, Rh, and Pd; The active component B is at least one of Ni, Fe, Co, Mo, Pt, Ru, Rh, Pd, Cu, Zn, and Al; The carrier is at least one of CaO, MgO, Ca(OH)2, Mg(OH)2, Li2ZrO3, Li2SiO3, Li4SiO4, zeolite, hydrotalcite or molecular sieve.

2. The three-way catalyst for in-situ carbon capture and conversion according to claim 1, characterized in that: The mass ratio of the active component A to the active component B is 1:(0.1-10), and the mass ratio of the active component A to the carrier is 1:(1-10000).

3. A method for preparing a three-way catalyst for in-situ carbon capture and conversion according to claim 1 or 2, characterized in that: The active component A, the active component B and the carrier are compounded to obtain the active component A, the active component B and the carrier.

4. Use of the three-way catalyst for in-situ carbon capture and conversion as claimed in claim 1 or 2 in catalyzing steam reforming reaction of organic matter and / or catalyzing in-situ conversion reaction of CO2.

5. An in-situ carbon capture and conversion method based on the three-way catalyst according to claim 1, characterized in that: The three-way catalyst is used to catalyze the steam reforming reaction of organic matter. When the concentration of CO2 in the product remains unchanged, the steam reforming reaction of organic matter is stopped, and the three-way catalyst is switched to catalyze the in-situ conversion reaction of CO2. In the in-situ conversion reaction of catalyzing CO2, when the concentration of the target product does not change, the three-way catalyst is switched to catalyze the steam reforming reaction of organic matter, and the above-mentioned operations of catalyzing the steam reforming reaction of organic matter and catalyzing the in-situ conversion reaction of CO2 are repeated.

6. The in-situ carbon capture and conversion method of a three-way catalyst according to claim 5, characterized in that: In the organic matter steam reforming reaction, the molar ratio of water vapor to hydrocarbon is (1-10):1, and the space velocity is 1-360000m 3 h -1 , the reaction temperature is 100-1000℃, and the reaction pressure range is 1-30bar; The temperature of the catalytic CO2 in-situ conversion reaction is 100-1000°C, and the reaction pressure ranges from 1-30 bar.

7. The in-situ carbon capture and conversion method of a three-way catalyst according to claim 5, characterized in that: The catalytic CO2 in-situ conversion reaction includes a CO2 hydrogenation reaction and a CO2 dry reforming reaction.

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