Solar-driven thermochemical cascade reaction to crack carbon dioxide to produce fuel

Abstract

The solar-driven thermochemical cascade reaction cracking carbon dioxide fuel production device belongs to the field of solar thermochemical technology. The existing cracking carbon dioxide process has the problems of high reaction temperature and low conversion efficiency. The dish-type solar concentrator is used to gather sunlight and irradiate the gathered sunlight to the high-temperature reaction zone in the reactor. Part of the sunlight entering the high-temperature reaction zone irradiates the surface of the No. 1 foam ceramic, and the other part passes through the pores of the No. 1 foam ceramic and irradiates the graphite sheet. The graphite sheet absorbs the heat of the sunlight and conducts the heat to the No. 2 foam ceramic; one end on the same side of the low-temperature reaction zone and the high-temperature reaction zone respectively opens a 1:1 methane and water raw gas inlet and a CO product outlet; the other end on the same side of the low-temperature reaction zone and the high-temperature reaction zone respectively opens a synthesis gas product outlet and a carbon dioxide raw gas inlet; the carbon dioxide raw gas inlet and the synthesis gas product outlet are connected to the gas pipe fittings. Used for cracking carbon dioxide.

Description

Technical Field

[0001] The invention relates to a fuel preparation device for cracking CO2, belonging to the technical field of solar thermal chemistry. Background Art

[0002] At present, my country's energy consumption is mainly based on fossil fuels, which account for about 85% of the total energy consumption, while renewable energy consumption is only about 3%, which greatly restricts the reform of energy structure and sustainable development of social economy. Faced with the increasingly severe energy resource situation and global environmental problems, how to develop efficient and clean energy technologies to achieve the coordinated and sustainable development of the natural environment and human society has become the primary goal of the international community to rationally dispatch energy resources and carry out carbon emission reduction work. Among them, solar thermochemical technology focuses solar energy as a heat source, drives high-temperature endothermic reactions, and converts and stores solar radiation in the form of chemical energy with high density, which is considered to be the future clean energy technology. This technology effectively combines the two advantages of efficient utilization of solar energy and carbon-based energy recovery, providing a new research idea for solving the greenhouse effect and energy shortage problems at the same time.

[0003] The ultimate goal of solar thermochemical technology is to produce hydrogen or synthesis gas products. The main components of synthesis gas are H2 and CO, which can be directly used as fuel or raw gas for various chemical products. It plays an extremely important role in the chemical industry. With the main greenhouse gases CO2 and CH4 as raw materials, there are currently three thermochemical technology pathways that can convert them into hydrogen or synthesis gas products: (1) methane wet reforming reaction; (2) methane dry reforming reaction; (3) two-step redox cycle reaction. The reaction temperatures required for the above three reaction systems increase in sequence, and the degree of industrialization decreases in sequence. Among them, the methane wet reforming reaction uses CH4 and H2O as raw materials. At a reaction temperature of about 700℃, a synthesis gas product with a theoretical ratio of H2:CO=3:1 can be produced. It is the main technical route for industrial hydrogen production. The amount of hydrogen produced by this reaction exceeds 50 million tons per year, accounting for 2%-5% of the global energy consumption, and has a very high technical maturity. The methane dry reforming reaction uses CH4 and CO2 as raw materials, and the industrial reaction temperature is between 800-1000℃. Its main advantage is that it can produce synthesis gas with a theoretical H2:CO=1:1, which is suitable as a raw material for reprocessing in various chemical processes using the Fischer-Tropsch synthesis method. The operating temperature required for the two-step redox cycle reaction is usually 1200-1800℃. Its outstanding advantage is that it can directly crack H2O or CO2, but the harsh high-temperature reaction conditions have resulted in no mature reaction device design. Up to now, the energy efficiency of the relevant system is still less than 6%. Therefore, the existing methods of producing synthesis gas have problems such as low energy efficiency, high reaction temperature, poor continuity, and low conversion efficiency, which seriously limit the actual engineering application. Summary of the invention

[0004] The purpose of the present invention is to solve the problems of high reaction temperature and low conversion efficiency in the related process of cracking carbon dioxide to produce fuel by the existing high-temperature thermochemical method, and proposes a solar-driven thermochemical cascade reaction cracking carbon dioxide to produce fuel device.

[0005] A solar-driven thermochemical cascade reaction cracking device for producing fuel by carbon dioxide, the device comprising a dish-type solar concentrator, quartz glass, gas pipe fittings, graphite sheets, No. 1 foam ceramic, No. 2 ceramic and a reactor;

[0006] The No. 1 foam ceramic is a ceramic body with a porous foam structure, and the surface of the No. 1 foam ceramic is coated with a No. 1 catalytic material;

[0007] The second foam ceramic is a ceramic body with a porous foam structure, and the surface of the second foam ceramic is coated with a second catalytic material;

[0008] The inside of the reactor is divided into a high-temperature reaction zone and a low-temperature reaction zone by a graphite sheet, and the high-temperature reaction zone is located at the opening side of the reactor, and the low-temperature reaction zone is located at the bottom side of the reactor; the first foam ceramic is arranged in the high-temperature reaction zone; the second foam ceramic is arranged in the low-temperature reaction zone;

[0009] One end of the reactor is open, and a quartz glass cover is closed at the opening of the reactor. A dish-type solar concentrator is located outside the quartz glass, and the dish-type solar concentrator is placed toward the quartz glass. The dish-type solar concentrator is used to collect sunlight and irradiate the collected sunlight to the high-temperature reaction zone in the reactor. A part of the sunlight entering the high-temperature reaction zone irradiates the surface of the first foam ceramic, and another part passes through the pores of the first foam ceramic and irradiates the graphite sheet. The graphite sheet absorbs the heat of the sunlight and conducts the heat to the second foam ceramic.

[0010] A 1:1 CH4 and H2O raw gas inlet is opened on one side of the low-temperature reaction zone; a CO product outlet is opened on the high-temperature reaction zone on the same side as the 1:1 CH4 and H2O raw gas inlet; a synthesis gas product outlet is opened on the other side of the low-temperature reaction zone; a CO2 raw gas inlet is opened on the high-temperature reaction zone on the same side as the synthesis gas product outlet; the CO2 raw gas inlet and the synthesis gas product outlet are connected to gas pipes.

[0011] Preferably, the graphite sheet is arc-shaped;

[0012] The arc-shaped concave surface is opposite to the high-temperature reaction zone, and the arc-shaped convex surface is opposite to the low-temperature reaction zone.

[0013] Preferably, the device further comprises a pneumatic valve;

[0014] The pneumatic valve is arranged on the gas line pipe fitting; the pneumatic valve is used to control the opening or closing of the synthesis gas product outlet.

[0015] Preferably, the device further comprises a gas flow controller;

[0016] The gas flow controller is arranged on the gas line pipe fitting; the gas flow controller is used to control the flow rate of the synthesis gas introduced into the CO2 raw gas inlet.

[0017] Preferably, the device further comprises a stainless steel housing and an alumina thermal insulation layer;

[0018] The outer wall of the reactor is a two-layer structure, which comprises an alumina insulation layer and a stainless steel shell from the inside to the outside.

[0019] The beneficial effects of the present invention are:

[0020] Combining the technical advantages of methane wet reforming reaction and two-step redox cycle reaction, the present application designs a direct / indirect hybrid heating device structure. The technical core of the present application is: (1) cascade utilization of solar energy: a high-throughput concentrated solar energy is directly irradiated to the high-temperature reaction zone, and a two-step redox cycle reaction is carried out in the direct heating chamber (high-temperature reaction zone, about 1200°C), while a methane wet reforming reaction is carried out in the indirect heating chamber (low-temperature reaction zone, about 800°C); (2) cascade utilization of chemical reactions: the product of the low-temperature reaction zone (theoretically, a synthesis gas with a ratio of H2:CO=3:1) is introduced into the high-temperature reaction zone as an auxiliary gas, and the reducing H2 therein is used to reduce CO2 to CO in situ, thereby significantly reducing the reaction temperature and greatly improving the CO2 conversion rate.

[0021] Therefore, compared with the prior art, the present application requires a lower reaction temperature, better continuity, higher energy efficiency, higher conversion efficiency, and the gas products can be directly separated due to the reasonable device structure.

[0022] Based on the above technical route, a small amount of CH4 gas can be used to achieve the cracking and reduction of a large amount of CO2, and the solar energy can be efficiently stored as chemical energy in the synthesis gas product. At the same time, it is expected to break through the current solar-fuel conversion efficiency in the field of high-temperature thermochemistry and promote the industrialization process of CO2 resource utilization.

[0023] This application proposes for the first time a solar-driven thermochemical cascade reaction cracking CO2 fuel production device, which combines the technical advantages of methane wet reforming and two-step redox cycle reaction, can efficiently recycle carbon waste gas and convert it into high-value-added solar fuel, with tangible social and environmental economic benefits. This application has important theoretical and practical significance for the resource utilization of CO2, efficient production of solar fuel, and the development of zero-carbon clean energy technology. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1This is a schematic diagram of the structure of a device for producing fuel by cracking carbon dioxide through solar-driven thermochemical cascade reactions. DETAILED DESCRIPTION

[0025] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0026] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments may be combined with each other.

[0027] The present invention will be further described below in conjunction with the accompanying drawings and specific embodiments, but they are not intended to limit the present invention.

[0028] Embodiment 1:

[0029] Combination Figure 1 This embodiment is described, a solar-driven thermochemical cascade reaction cracking carbon dioxide fuel production device, the device comprising a dish-type solar concentrator 1, quartz glass 4, gas pipe 6, graphite sheet 9, No. 1 foam ceramic, No. 2 ceramic and a reactor;

[0030] The No. 1 foam ceramic is a ceramic body with a porous foam structure, and the surface of the No. 1 foam ceramic is coated with a No. 1 catalytic material;

[0031] The second foam ceramic is a ceramic body with a porous foam structure, and the surface of the second foam ceramic is coated with a second catalytic material;

[0032] The inside of the reactor is divided into a high-temperature reaction zone 5 and a low-temperature reaction zone 12 by a graphite sheet 9, and the high-temperature reaction zone 5 is located at the opening side of the reactor, and the low-temperature reaction zone 12 is located at the bottom side of the reactor; the first foam ceramic is arranged in the high-temperature reaction zone 5; the second foam ceramic is arranged in the low-temperature reaction zone 12;

[0033] One end of the reactor is open, and a quartz glass 4 covers the opening of the reactor. A dish-type solar concentrator 1 is located outside the quartz glass 4, and the dish-type solar concentrator 1 is placed toward the quartz glass 4. The dish-type solar concentrator 1 is used to gather sunlight and irradiate the gathered sunlight to a high-temperature reaction zone 5 in the reactor. A portion of the sunlight entering the high-temperature reaction zone 5 irradiates the surface of the first foam ceramic, and another portion passes through the pores of the first foam ceramic and irradiates the graphite sheet 9. The graphite sheet 9 absorbs the heat of the sunlight and conducts the heat to the second foam ceramic.

[0034] A 1:1 CH4 and H2O raw gas inlet IV is opened on one side of the low-temperature reaction zone 12; a CO product outlet III is opened on the high-temperature reaction zone 5 on the same side as the 1:1 CH4 and H2O raw gas inlet IV; a synthesis gas product outlet II is opened on the other side of the low-temperature reaction zone 12; a CO2 raw gas inlet I is opened on the high-temperature reaction zone 5 on the same side as the synthesis gas product outlet II; the CO2 raw gas inlet I and the synthesis gas product outlet II are connected to the gas pipe 6.

[0035] In this embodiment, the pores of the No. 1 foam ceramic are larger than the pores of the No. 2 foam ceramic. The reason why the No. 1 foam ceramic has large pores is that sunlight can pass through the pores and transfer the sunlight to the graphite sheet to heat the graphite sheet.

[0036] Working principle:

[0037] The device uses solar energy as the driving source. The solar energy rays form high-flux irradiation after passing through the dish-type solar concentrator 1, and are transported to the reactor after passing through the high-temperature resistant quartz glass 4. After being absorbed by the No. 1 foam ceramic, a high-temperature environment is formed. Under the action of the catalyst on the surface of the No. 1 foam ceramic, a strong endothermic chemical reaction is stimulated, so that the catalyst generates MO x-δ , as shown in Formula 3, when carbon dioxide is introduced into the high temperature reaction zone, MO x-δ and CO2 to generate MO x and carbon monoxide. Under the barrier of the arc-shaped graphite sheet 9, the entire reaction chamber is divided into two reaction zones: the high-temperature reaction zone 5 is heated by direct high-flux solar radiation, the reaction temperature is about 1200°C, and the reaction type is a two-step redox cycle reaction based on an iron-based catalyst; the low-temperature reaction zone 12 is heated by indirect heating through the high-thermal conductivity arc-shaped graphite sheet 9, the reaction temperature is about 800°C, and the reaction type is a methane wet reforming reaction based on a nickel-based catalyst. The purpose of designing the graphite sheet into an arc-shaped structure is to improve its thermomechanical strength while catering to the Gaussian distribution of concentrated solar energy, alleviate the heat concentration phenomenon in the central area, and make the temperature field distribution in the two reaction zones more uniform, thereby improving the chemical conversion efficiency.

[0038] Reaction principle: The starting end of the whole reaction is the CH4 and H2O raw gas inlet IV, which undergoes wet reforming reaction (Formula 1) in the low-temperature reaction zone 12 to form a synthesis gas product - H2 and CO in a theoretical ratio of 3:1. Under the control of the pneumatic valve 8, part of the synthesis gas is directly sent out from the synthesis gas product outlet II as the final product, and the other part of the synthesis gas is mixed with the CO2 raw gas in the inlet I under the precise control of the gas flow controller 7, and then sent to the high-temperature reaction zone 5 for high-temperature cracking reaction of CO2 (Formulas 2, 3, 4), and the final product CO is output from the outlet III.

[0039] Overall reaction of methane wet reforming:

[0040] CH4+H2O→CO+3H2 (Formula 1)

[0041] Two-step redox cycle reaction (M represents the metal element, δ is the stoichiometric number of CO2, and x is a positive integer):

[0042] Reduction steps: MO x →MO x-δ +0.5δO2 (Formula 2) Oxidation step: MO x-δ +δCO2→MO x +δCO (Formula 3) Overall reaction: CO2→0.5O2+CO (Formula 4)

[0043] The technical core of this reaction device has two points: first, through the design structure that combines direct heating and indirect heating, the cascade utilization of solar energy is realized to ensure the simultaneous implementation of the two-step redox cycle in the high-temperature zone and the methane wet reforming reaction in the low-temperature zone; second, the H2 in the methane wet reforming product is used to create a reducing atmosphere in the high-temperature reaction zone, thereby lowering the reduction temperature required for the two-step reaction, achieving rapid cracking of CO2 through cascade reactions and improving the overall reaction efficiency of the system.

[0044] In addition, the present application aims at the heat transfer and chemical reaction characteristics of the high-temperature and low-temperature reaction zones, respectively filling the No. 1 foam ceramic (favorable for heat radiation transmission during direct heating) and No. 2 foam ceramic (favorable for heat conduction and heat convection during indirect heating) with surface-coated catalysts, which can increase the reaction area while strengthening the heat and mass transfer and gas-solid interface exchange in the reaction zone, thereby improving the reaction efficiency. At the same time, the shape design of the arc-shaped graphite sheet can well alleviate the heat concentration phenomenon of high-flux concentrated solar radiation at the center of the foam ceramic, while improving the thermomechanical strength and making the temperature distribution of the reaction zones on both sides more uniform, promoting the chemical conversion efficiency.

[0045] Compared with the traditional high-temperature thermochemical reduction of CO2 technology, the advantages of the present invention are: (1) with the assistance of a small amount of additional hydrogen source (CH4 gas), efficient and green reduction of a large amount of CO2 can be achieved; (2) the reaction temperature required for cracking CO2 is lower, and it is expected that the reaction temperature of the conventional two-step reduction of CO2 can be reduced by more than 300°C; (3) there is no need to separate the product gas again, and synthesis gas and CO can be directly obtained at the two gas outlets; (4) Cascade utilization is achieved in both thermal energy and chemical reaction, which is conducive to further improving the overall energy conversion efficiency of the system.

[0046] In the present application, the pores on the No. 1 foam ceramic inside the high temperature reaction zone 5 are larger than the pores on the No. 2 foam ceramic inside the low temperature reaction zone 11. The material of the quartz glass 4 is a high temperature resistant material.

[0047] In a preferred embodiment, the graphite sheet 9 is arc-shaped;

[0048] The arc-shaped concave surface is opposite to the high-temperature reaction zone 5 , and the arc-shaped convex surface is opposite to the low-temperature reaction zone 12 .

[0049] In a preferred embodiment, the device further comprises a pneumatic valve 8;

[0050] The pneumatic valve 8 is arranged on the gas line pipe 6; the pneumatic valve 8 is used to control the opening or closing of the synthesis gas product outlet II.

[0051] In a preferred embodiment, the device further comprises a gas flow controller 7;

[0052] The gas flow controller 7 is arranged on the gas line pipe 6; the gas flow controller 7 is used to control the amount of synthesis gas introduced into the CO2 raw gas inlet I.

[0053] In a preferred embodiment, the device further comprises a stainless steel housing 10 and an alumina heat insulation layer 11;

[0054] The outer wall of the reactor is a two-layer structure, which comprises an alumina heat insulation layer 11 and a stainless steel shell 10 from the inside to the outside.

[0055] In this embodiment, the alumina thermal insulation layer 11 is a thermal insulation material.

[0056] In a preferred embodiment, the device further comprises a fixing member;

[0057] The quartz glass 4 is fixed to the stainless steel housing 9 by means of fixing parts.

[0058] In a preferred embodiment, the fixing member includes a fastening bolt 2 and a flange 3;

[0059] The flange 3 is arranged at the edge of the upper surface of the quartz glass 4 , and the fastening bolts 2 pass through the flange 3 and are fixed on the stainless steel shell 10 , so that the quartz glass 4 is clamped between the flange 3 and the stainless steel shell 9 .

[0060] In this embodiment, the main function of the fastening bolts 2 and the flange 3 is to fix the high temperature resistant quartz glass 4 .

[0061] A water cooling pipe may also be provided in the flange 3 to cool the quartz glass 4 .

[0062] In a preferred embodiment, the first foam ceramic and the second foam ceramic are both silicon carbide foam ceramics;

[0063] The first catalytic material is an iron-based catalyst, and the second catalytic material is a nickel-based catalyst.

[0064] In this embodiment, silicon carbide foam ceramics are ceramic bodies with porous foam structures after firing silicon carbide powder. The structures of foam ceramics and silicon carbide foam ceramics are both existing structures.

[0065] In a preferred embodiment, a methane wet reforming reaction occurs in the low-temperature reaction zone 11 based on a nickel-based catalyst; and a two-step redox cycle reaction occurs in the high-temperature reaction zone 5 based on an iron-based catalyst.

[0066] A preferred embodiment is methane wet reforming reaction:

[0067] CH4+H2O→CO+3H2 formula 1,

[0068] Reduction reaction:

[0069] MO x →MO x-δ +0.5δO2 formula 2,

[0070] Oxidation reaction:

[0071] MO x-δ +δCO2→MO x +δCO formula 3,

[0072] Where, δ is the stoichiometric coefficient of CO2; M is the metal element; x is a positive integer;

[0073] Overall reaction:

[0074] CO2→0.5O2+CO formula 4.

[0075] In this embodiment, MO x The iron-based catalyst inside the high-temperature reaction zone 5 is a metal oxide. The metal oxide undergoes a reduction reaction, and the reduced metal oxide obtained is used in an oxidation reaction to capture oxygen atoms in CO2 and finally obtain CO.

[0076] The technical core of this reaction device has two points: first, through the design structure that combines direct heating and indirect heating, the cascade utilization of solar energy is realized to ensure the simultaneous implementation of the two-step redox cycle in the high-temperature zone and the methane wet reforming reaction in the low-temperature zone; second, the H2 in the methane wet reforming product is used to create a reducing atmosphere in the high-temperature reaction zone, thereby lowering the reduction temperature required for the two-step reaction, achieving rapid cracking of CO2 through cascade reactions and improving the overall reaction efficiency of the system.

[0077] Although the present invention is described herein with reference to specific embodiments, it should be understood that these embodiments are merely examples of the principles and applications of the present invention. It should therefore be understood that many modifications may be made to the exemplary embodiments and that other arrangements may be devised without departing from the spirit and scope of the present invention as defined by the appended claims. It should be understood that the various dependent claims and features described herein may be combined in a manner different from that described in the original claims. It should also be understood that features described in conjunction with individual embodiments may be used in other described embodiments.

Claims

1. A solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel, characterized in that: The device comprises a dish-type solar concentrator (1), quartz glass (4), a gas path pipe (6), a graphite sheet (9), a first foam ceramic, a second ceramic and a reactor; The No. 1 foam ceramic is a ceramic body with a porous foam structure, and the surface of the No. 1 foam ceramic is coated with a No. 1 catalytic material; The second foam ceramic is a ceramic body with a porous foam structure, and the surface of the second foam ceramic is coated with a second catalytic material; The interior of the reactor is divided into a high-temperature reaction zone (5) and a low-temperature reaction zone (12) by a graphite sheet (9), wherein the high-temperature reaction zone (5) is located at the opening side of the reactor and the low-temperature reaction zone (12) is located at the bottom side of the reactor; a No. 1 foam ceramic is arranged in the high-temperature reaction zone (5); and a No. 2 foam ceramic is arranged in the low-temperature reaction zone (12); One end of the reactor is open, and a quartz glass (4) covers the opening of the reactor. A dish-type solar concentrator (1) is located outside the quartz glass (4), and the dish-type solar concentrator (1) is placed toward the quartz glass (4). The dish-type solar concentrator (1) is used to collect sunlight and irradiate the collected sunlight to a high-temperature reaction zone (5) in the reactor. A portion of the sunlight entering the high-temperature reaction zone (5) is irradiated to the surface of the first foam ceramic, and another portion passes through the pores of the first foam ceramic and is irradiated to the graphite sheet (9). The graphite sheet (9) absorbs the heat of the sunlight and conducts the heat to the second foam ceramic. A CH4 and H2O raw gas inlet (IV) is provided on one side of the low-temperature reaction zone (12); a CO product outlet (III) is provided on the high-temperature reaction zone (5) on the same side as the CH4 and H2O raw gas inlet (IV); a synthesis gas product outlet (II) is provided on the other side of the low-temperature reaction zone (12); a CO2 raw gas inlet (I) is provided on the high-temperature reaction zone (5) on the same side as the synthesis gas product outlet (II); and the CO2 raw gas inlet (I) and the synthesis gas product outlet (II) are connected to a gas circuit pipe (6).

2. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 1 is characterized in that: The graphite sheet (9) is arc-shaped; The arc-shaped concave surface is opposite to the high-temperature reaction zone (5), and the arc-shaped convex surface is opposite to the low-temperature reaction zone (12).

3. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 1, characterized in that: The device also includes a pneumatic valve (8); The pneumatic valve (8) is arranged on the gas line pipe (6); the pneumatic valve (8) is used to control the opening or closing of the synthesis gas product outlet (II).

4. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 1, characterized in that: The device also includes a gas flow controller (7); The gas flow controller (7) is arranged on the gas line pipe (6); the gas flow controller (7) is used to control the flow rate of the synthesis gas introduced into the CO2 raw gas inlet (I).

5. The solar-driven thermochemical cascade reaction cracking carbon dioxide fuel production device according to claim 1 is characterized in that: The device also includes a stainless steel housing (10) and an alumina heat insulation layer (11); The outer wall of the reactor is a two-layer structure, which comprises an alumina heat insulation layer (11) and a stainless steel shell (10) from the inside to the outside.

6. The solar-driven thermochemical cascade reaction cracking carbon dioxide fuel production device according to claim 1 is characterized in that: The device also includes a fixing member; The quartz glass (4) is fixed on the stainless steel housing (10) by means of a fixing piece.

7. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 6, characterized in that: The fixing member comprises a fastening bolt (2) and a flange (3); The flange (3) is arranged at the edge of the upper surface of the quartz glass (4), and the fastening bolts (2) pass through the flange (3) and are fixed on the stainless steel shell (10), so that the quartz glass (4) is clamped between the flange (3) and the stainless steel shell (10).

8. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 1, characterized in that: The No. 1 foam ceramic and the No. 2 foam ceramic are both silicon carbide foam ceramics; The first catalytic material is an iron-based catalyst, and the second catalytic material is a nickel-based catalyst.

9. The solar-driven thermochemical cascade reaction device for cracking carbon dioxide to produce fuel according to claim 8, characterized in that: In the low temperature reaction zone (12), a methane wet reforming reaction takes place based on a nickel-based catalyst; In the high temperature reaction zone (5), a two-step redox cycle reaction occurs based on an iron-based catalyst.

10. The solar-driven thermochemical cascade reaction carbon dioxide cracking fuel production device according to claim 9, characterized in that: Methane wet reforming reaction: CH4+H2O→CO+3H2 formula 1, Reduction reaction: MO x →MO x-δ +0.5δO2 Formula 2, Oxidation reaction: MO x-δ +δCO2 →MO x +δCO formula 3, In Formula 2 and Formula 3, δ is the stoichiometric coefficient of CO2; M is the metal element; x is a positive integer; Overall reaction: CO2→0.5O2+CO formula 4.

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