System and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction

Abstract

The present invention discloses a system and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, with carbon dioxide and methane as raw materials, wherein the system comprises: a riser reactor, a catalyst stripping tower, a heat exchanger, a first gas supply mechanism, a liquid supply mechanism, a second gas supply mechanism and a condenser. The riser reactor contains a catalyst, and the riser reactor is used to reform the chemical reaction of carbon dioxide and methane to obtain a catalyst and a first mixed gas after the reaction. The catalyst stripping tower is connected to the riser reactor, and the catalyst stripping tower is used to strip and clean the carbon deposits on the surface of the catalyst after the reaction to obtain a catalyst and a second mixed gas. The heat exchanger is connected to the riser reactor and the catalyst stripping tower, respectively. The technical solution of the embodiment of the present invention is low-carbon and environmentally friendly, and the industrial production of synthesis gas is used to produce methanol or SAF to meet market demand, and the energy utilization efficiency is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen production, and in particular to a system and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction. Background Art

[0002] Carbon capture and utilization (CCU) and carbon capture and storage (CCS) are both considered important strategies for reducing carbon dioxide emissions.

[0003] Carbon capture and storage (CCS) mainly captures carbon dioxide produced by the combustion of fossil fuels and stores it in geological structures and deep sea waters for a long time, but the intensity of fossil fuel consumption remains basically unchanged. Carbon capture and utilization (CCU) is the capture and reuse of carbon dioxide produced by the combustion of fossil fuels, which is equivalent to the reuse of waste. Through chemical reactions, hydrocarbon products are generated to become alternative resources for petrochemical raw materials and fossil fuels, and the economic benefits of resource use and the intensity of fossil fuel consumption are reduced.

[0004] Solar thermal energy is used to convert carbon captured carbon dioxide into synthesis gas for the production of methanol or SAF. Methanol and SAF are both stable substances and fuels for the storage and transportation of green energy. Methanol can be converted into ethylene or propylene through methanol to olefins technology, replacing traditional distillation cracking and reducing fossil raw material consumption and energy consumption. Summary of the invention

[0005] The purpose of the present invention is to provide a system and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, which uses carbon dioxide and methane as raw materials and optimizes the use of steam to produce synthesis gas. It is low-carbon and environmentally friendly. The industrial production of synthesis gas is used to produce methanol or SAF to meet market demand, and improves energy utilization efficiency.

[0006] To achieve the above-mentioned object, in a first aspect, the present invention provides a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, with carbon dioxide and methane as raw materials, and the system comprises: a riser reactor, a catalyst stripping tower, a heat exchanger, a first gas supply mechanism, a liquid supply mechanism, a second gas supply mechanism and a condenser. The riser reactor contains a catalyst, and the riser reactor is used to reform the chemical reaction of carbon dioxide and methane to obtain a catalyst and a first mixed gas after the reaction. The catalyst stripping tower is connected to the riser reactor, and the catalyst stripping tower is used to strip and clean the carbon deposits on the surface of the catalyst after the reaction to obtain a catalyst and a second mixed gas. The heat exchanger is connected to the riser reactor. The first gas supply mechanism is connected to the heat exchanger, and the first gas supply mechanism is used to provide a first gas to the riser reactor through the heat exchanger, so as to catalyze the reaction with the catalyst. The liquid supply mechanism is connected to the riser reactor, and the liquid supply mechanism is used to provide hot liquid to the riser reactor. The second gas supply mechanism is connected to the catalyst stripping tower, and the second gas supply mechanism is used to provide a second gas to the catalyst stripping tower, and the second gas is used to strip the reduced catalyst. One end of the condensing tank is connected to the heat exchanger, and the other end of the condensing tank is connected to the liquid supply mechanism, and the condensing tank is used to receive the first mixed gas and the second mixed gas to generate synthesis gas.

[0007] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a high-temperature focusing mechanism and a light-transmitting mirror. The high-temperature focusing mechanism is used to provide solar heat and is located above the liquid supply mechanism; and the light-transmitting mirror is arranged on the top of the liquid supply mechanism, and the light-transmitting mirror is used to receive the solar heat provided by the high-temperature focusing mechanism and introduce the solar heat into the liquid supply mechanism, thereby heating the molten salt in the liquid supply mechanism to form the hot liquid.

[0008] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes an air cooler, one end of the air cooler is connected to the heat exchanger, and the other end of the air cooler is connected to the condensation tank.

[0009] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a first pipeline, a second pipeline, a third pipeline, a fourth pipeline and a fifth pipeline. One end of the first pipeline is connected to the first gas supply mechanism, and the other end of the first pipeline is connected to the heat exchanger. One end of the second pipeline is connected to the heat exchanger, and the other end of the second pipeline is connected to the bottom of the riser reactor. One end of the third pipeline is connected to the upper part of the riser reactor, and the other end of the third pipeline is connected to the catalyst stripping tower. One end of the fourth pipeline is connected to the bottom of the catalyst stripping tower, and the other end of the fourth pipeline is connected to the lower part of the riser reactor. And one end of the fifth pipeline is connected to the second gas supply mechanism, and the other end of the fifth pipeline is connected to the lower part of the catalyst stripping tower.

[0010] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a first gas-solid separator, a second gas-solid separator and a sixth pipeline. The first end of the first gas-solid separator is connected to the riser reactor through the third pipeline, and the second end of the first gas-solid separator is connected to the catalyst stripping tower. The first end of the second gas-solid separator is connected to the third end of the first gas-solid separator, and the second end of the second gas-solid separator is connected to the catalyst stripping tower. And one end of the sixth pipeline is connected to the third end of the second gas-solid separator, and the other end of the sixth pipeline is connected to the heat exchanger.

[0011] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a seventh pipeline and an eighth pipeline. One end of the seventh pipeline is connected to the liquid outlet of the liquid supply mechanism, and the other end of the seventh pipeline is connected to the lower part of the riser reactor. And one end of the eighth pipeline is connected to the liquid return port of the liquid supply mechanism, and the other end of the eighth pipeline is connected to the upper part of the riser reactor.

[0012] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction also includes a ninth pipeline, a tenth pipeline, an eleventh pipeline and a condensate pump. One end of the ninth pipeline is connected to the heat exchanger, and the other end of the ninth pipeline is connected to the air cooler. One end of the tenth pipeline is connected to the air cooler, and the other end of the tenth pipeline is connected to the condensate tank. One end of the eleventh pipeline is connected to the condensate tank, and the other end of the eleventh pipeline is connected to the liquid supply mechanism. And the condensate pump is arranged on the eleventh pipeline.

[0013] In one embodiment of the present invention, the first gas supply mechanism includes: a first gas supply unit, a second gas supply unit and a third gas supply unit. The first gas supply unit is used to provide methane, and the first gas supply unit is connected to the first pipeline through a twelfth pipeline. The second gas supply unit is used to provide carbon dioxide, and the second gas supply unit is connected to the first pipeline through a thirteenth pipeline. And the third gas supply unit is used to provide water vapor, and the third gas supply unit is connected to the first pipeline through a fourteenth pipeline.

[0014] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes a control mechanism, a first flow control valve, a second flow control valve, a third flow control valve, a fourth flow control valve, a first electronic valve and a second electronic valve. The first flow control valve is arranged on the twelfth pipeline, and the first flow control valve is electrically connected to the control mechanism. The second flow control valve is arranged on the thirteenth pipeline, and the second flow control valve is electrically connected to the control mechanism. The third flow control valve is arranged on the fourteenth pipeline, and the third flow control valve is electrically connected to the control mechanism. The fourth flow control valve is arranged on the fifth pipeline, and the fourth flow control valve is electrically connected to the control mechanism. The first electronic valve is arranged on the seventh pipeline, and the first electronic valve is electrically connected to the control mechanism. And the second electronic valve is arranged on the eighth pipeline, and the second electronic valve is electrically connected to the control mechanism.

[0015] In a second aspect, the present invention provides a method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction. Based on the above-mentioned system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, the method comprises:

[0016] adding a first gas into the riser reactor to fluidize the catalyst in the riser reactor;

[0017] supplying hot liquid to the riser reactor through a liquid supply mechanism to supply heat, so that the fluidized catalyst reacts chemically with the first gas to obtain a reacted catalyst and a first mixed gas;

[0018] The post-reaction catalyst is transported to a catalyst stripping tower, and a second gas is added to the catalyst stripping tower, so as to strip and clean the carbon deposits on the surface of the post-reaction catalyst to obtain a catalyst and a second mixed gas;

[0019] transporting the catalyst in the catalyst stripping tower to the riser reactor;

[0020] The first mixed gas and the second mixed gas are mixed and transported to a condensation tank to generate synthesis gas.

[0021] Compared with the prior art, the system and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to the present invention is low-carbon and environmentally friendly, recycles room temperature gas to industrially produce synthesis gas for producing methanol or SAF to meet market demand, and improves energy utilization efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a schematic diagram of a part of the structure of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 1 of the present invention;

[0023] Figure 2 This is another partial structural schematic diagram of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 1 of the present invention;

[0024] Figure 3 It is a schematic flow diagram of a method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Embodiment 2 of the present invention;

[0025] Figure 4 It is a schematic diagram of a part of the structure of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 3 of the present invention.

[0026] Description of main reference numerals:

[0027] 1-rising tube reactor, 2-catalyst stripping tower, 3-heat exchanger, 4-first gas supply mechanism, 5-liquid supply mechanism, 6-second gas supply mechanism, 7-condenser, 8-high temperature focusing mechanism, 9-air cooler, 10-first pipeline, 11-second pipeline, 12-third pipeline, 13-fourth pipeline, 14-fifth pipeline, 15-first gas-solid separator, 16-second gas-solid separator, 17-sixth pipeline, 18-seventh pipeline, 19-eighth pipeline, 20-ninth pipeline Pipeline, 21-the tenth pipeline, 22-the eleventh pipeline, 23-condensate pump, 24-the first air supply unit, 25-the second air supply unit, 26-the third air supply unit, 27-the first flow control valve, 28-the second flow control valve, 29-the third flow control valve, 30-the fourth flow control valve, 31-the first electronic valve, 32-the second electronic valve, 33-the twelfth pipeline, 34-the thirteenth pipeline, 35-the fourteenth pipeline, 36-control butterfly valve, 37-sliding valve. DETAILED DESCRIPTION

[0028] The embodiments of the present invention are further described in detail below in conjunction with the accompanying drawings and embodiments. It is to be understood that the specific embodiments described herein are only used to explain the embodiments of the present invention, rather than to limit the embodiments of the present invention. It is also necessary to explain that, for ease of description, only parts related to the embodiments of the present invention are shown in the accompanying drawings, rather than all structures.

[0029] To facilitate understanding, the main implementation concepts of the embodiments of the present invention are first briefly described.

[0030] The embodiment of the present invention utilizes the molten salt liquid heated by solar heat to heat the catalyst, reforms carbon dioxide and methane through chemical reactions, and produces synthesis gas (a mixture of hydrogen and carbon monoxide) as a raw material for downstream hydrocarbon synthesis devices (such as Fischer-Tropsch process devices) to produce sustainable renewable aviation fuel SAF. Since the embodiment of the present invention is based on renewable energy and raw materials, it is not limited by the supply of raw materials, and industrial production can meet the market demand for SAF.

[0031] Thermochemical reforming reactions based on cerium dioxide or aluminum oxide as carriers and transition metals or their alloys including (but not limited to) nickel, palladium, iridium, platinum, ruthenium, rhodium, etc. as catalysts can efficiently utilize the heat provided by solar energy to produce synthesis gas, and the metal oxide carriers and transition metal catalysts selected in the embodiments of the present invention include but are not limited to cerium dioxide, nickel, etc.

[0032] Embodiment 1

[0033] Figure 1 This is a schematic diagram of a part of the structure of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 1 of the present invention. Figure 2 FIG. 1 is another schematic diagram of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 1 of the present invention. Figure 1 to Figure 2 As shown, Example 1 provides a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, using carbon dioxide and methane as raw materials, and the system includes: a riser reactor 1, a catalyst stripping tower 2, a heat exchanger 3, a first gas supply mechanism 4, a liquid supply mechanism 5, a second gas supply mechanism 6 and a condenser 7.

[0034] The riser reactor 1 contains a catalyst, and the riser reactor 1 is used for chemical reaction of reforming carbon dioxide and methane to obtain a catalyst and a first mixed gas after the reaction;

[0035] Specifically, the catalyst uses metallic nickel with cerium dioxide (CeO2) as a carrier; wherein the first mixed gas includes hydrogen and carbon monoxide.

[0036] The catalyst stripping tower 2 is connected to the riser reactor 1, and the catalyst stripping tower 2 is used to strip and clean the carbon deposits on the surface of the catalyst after the reaction to obtain the catalyst and the second mixed gas;

[0037] Specifically, the catalyst stripping tower 2 strips the catalyst after the reaction to remove carbon deposits by adding a second gas, thereby restoring the activity of the catalyst so that it can be recycled. In this process, not only the catalyst is stripped, but also a second mixed gas is generated, which enters the subsequent process together with the first mixed gas generated by the riser reactor 1 to finally generate synthesis gas. This design realizes the effective recycling of the catalyst and improves the overall efficiency and economy of the system; wherein the second mixed gas includes hydrogen and carbon monoxide. Among them, the catalyst stripping tower has a stripping section, the stripping section uses a grid filler, and the stripping section is used to provide a physical surface for catalyst stripping. Among them, a control butterfly valve 36 is provided at the top of the riser reactor 1, and the control butterfly valve 36 can be, for example, a pneumatic butterfly valve. When the pressure inside the riser reactor 1 is too high, the control butterfly valve 36 automatically opens; and when the pressure inside the riser reactor 1 returns to normal, the control butterfly valve 36 automatically closes.

[0038] The heat exchanger 3 is connected to the riser reactor 1;

[0039] Specifically, the main function of the heat exchanger 3 connected to the riser reactor 1 is to transfer heat to the gas entering the riser reactor 1 through the heat exchange process, so as to ensure that the catalyst in the riser reactor 1 can be efficiently operated under suitable temperature conditions. This connection design not only improves the utilization efficiency of thermal energy, but also helps to maintain the stability and controllability of the reaction process.

[0040] The first gas supply mechanism 4 is connected to the heat exchanger 3, and the first gas supply mechanism 4 is used to provide the first gas to the riser reactor 1 through the heat exchanger 3, so as to perform a catalytic reaction with the catalyst;

[0041] Specifically, the first gas supply mechanism 4 is closely connected to the heat exchanger 3. The first gas preheated by the heat exchanger 3 is accurately fed into the riser reactor 1 to undergo an efficient catalytic reaction with the fluidized catalyst. This process ensures that the reaction system is maintained at an optimal temperature state and promotes the smooth progress of the catalytic reaction.

[0042] The liquid supply mechanism 5 is connected to the riser reactor 1, and the liquid supply mechanism 5 is used to provide hot liquid to the riser reactor 1;

[0043] Specifically, the liquid supply mechanism 5 is directly connected to the riser reactor 1 and is responsible for stably delivering high-temperature hot liquid into the reactor. The hot liquid serves as a heat source to provide necessary heat energy for the catalytic reaction in the riser, ensuring that the reaction proceeds efficiently under suitable temperature conditions.

[0044] The second gas supply mechanism 6 is connected to the catalyst stripping tower 2, and the second gas supply mechanism 6 is used to provide a second gas to the catalyst stripping tower 2, and the second gas is used to strip the post-reaction catalyst;

[0045] Specifically, the second gas supply mechanism 6 is tightly connected to the catalyst stripping tower 2, and its main function is to provide the stripping tower with a specific second gas, which interacts with the reacted catalyst in the stripping tower, and effectively removes carbon deposits on the catalyst surface through the stripping process, thereby restoring the activity of the catalyst and preparing for subsequent catalytic reactions.

[0046] One end of the condensation tank 7 is connected to the heat exchanger 3, and the other end of the condensation tank 7 is connected to the liquid supply mechanism 5, and the condensation tank 7 is used to receive the first mixed gas and the second mixed gas to generate synthesis gas;

[0047] Specifically, one end of the condenser tank 7 is connected to the heat exchanger 3, and the other end is connected to the liquid supply mechanism 5. The main task of the condenser tank 7 is to receive the first mixed gas from the heat exchanger 3 and the second mixed gas from the catalyst stripping tower 2, condense the water vapor and other condensable components in the mixed gas through the condensation process, thereby generating pure synthesis gas, and the generated condensate is returned to the liquid supply mechanism 5 for recycling.

[0048] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a high-temperature focusing mechanism 8 and a light-transmitting mirror. The high-temperature focusing mechanism 8 is used to provide solar heat and is located above the liquid supply mechanism 5; and the light-transmitting mirror is arranged on the top of the liquid supply mechanism 5, and the light-transmitting mirror is used to receive the solar heat provided by the high-temperature focusing mechanism 8 and introduce the solar heat into the liquid supply mechanism 5, thereby heating the molten salt in the liquid supply mechanism 5 to form the hot liquid.

[0049] Specifically, the present invention cleverly utilizes solar energy as a heat source. The high-temperature focusing mechanism 8 is located above the liquid supply mechanism 5 to concentrate and focus the solar heat, and the light-transmitting mirror is like a bridge, which accurately introduces the high-intensity solar heat captured by the focusing mechanism into the liquid supply mechanism 5, and directly and efficiently heats the molten salt circulating inside, thereby generating high-temperature hot liquid. This process not only realizes the efficient utilization of clean energy, but also significantly reduces the operating cost of the system, reflecting the advanced concept of low-carbon and environmental protection. Among them, the light-transmitting mirror is made of high-temperature resistant quartz glass, and flexible carbon fibers are arranged inside the glass, which can significantly enhance the strength of the quartz glass without affecting the light transmission of the glass, and the diameter of the light-transmitting mirror is 1 / 4-1 / 2 of the diameter of the liquid supply mechanism 5, and the preferred value is 1 / 3, which can effectively reduce the high-temperature radiation inside the liquid supply mechanism 5.

[0050] In a specific embodiment, the molten salt is heated by sunlight, and the temperature rises to 700°C. A part of the molten salt at 700°C enters the sleeve of the riser reactor 1 through the seventh pipeline 18 to heat the catalyst. The molten salt temperature drops to about 680°C and returns to the liquid supply mechanism 5 through the eighth pipeline 19 for continued heating and recycling. Another part of the molten salt at 700°C is used to heat the condensate delivered by the condensate pump 23 into water vapor, which is returned to the riser reactor 1 and the catalyst stripping tower 2 for recycling. Another part of the molten salt at 700°C is temporarily stored in the liquid supply mechanism 5. When there is no sunlight or at night, the stored molten salt at 700°C is used to heat the catalyst and generate water vapor. A cold and hot molten salt pump is set in the liquid supply mechanism 5 for the transportation of molten salt. Among them, the riser reactor 1 is a sleeve structure, with catalysts and reaction gases inside, and molten salt is carried in the jacket. Among them, the seventh pipeline 18 and the eighth pipeline 19 can also be connected by a pipeline, and a bypass regulating valve (electrically connected to the control structure) is provided on the pipeline. When the temperature in the lifting pipe jacket is higher than the set value, the bypass regulating valve can be opened to reduce the flow rate of molten salt entering the jacket, thereby adjusting the temperature in the jacket.

[0051] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction also includes an air cooler 9, one end of the air cooler 9 is connected to the heat exchanger 3, and the other end of the air cooler 9 is connected to the condensation tank 7.

[0052] Specifically, the addition of the air cooler 9 further improves the thermal management efficiency of the system. The air cooler 9 is located between the heat exchanger 3 and the condensation tank 7. Through air cooling, the temperature of the high-temperature gas flowing out of the heat exchanger 3 is effectively reduced, creating favorable conditions for the subsequent condensation process, while ensuring the stable operation of the entire system.

[0053] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a first pipeline 10, a second pipeline 11, a third pipeline 12, a fourth pipeline 13 and a fifth pipeline 14. One end of the first pipeline 10 is connected to the first gas supply mechanism 4, and the other end of the first pipeline 10 is connected to the heat exchanger 3. One end of the second pipeline 11 is connected to the heat exchanger 3, and the other end of the second pipeline 11 is connected to the bottom of the riser reactor 1. One end of the third pipeline 12 is connected to the upper part of the riser reactor 1, and the other end of the third pipeline 12 is connected to the catalyst stripping tower 2. One end of the fourth pipeline 13 is connected to the bottom of the catalyst stripping tower 2, and the other end of the fourth pipeline 13 is connected to the lower part of the riser reactor 1. And one end of the fifth pipeline 14 is connected to the second gas supply mechanism 6, and the other end of the fifth pipeline 14 is connected to the lower part of the catalyst stripping tower 2.

[0054] Specifically, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction realizes efficient connection between various components through a carefully designed pipeline network. The first pipeline 10 to the fifth pipeline 14 are respectively responsible for the transportation of gas and catalyst: the first pipeline 10 guides the first gas from the gas supply mechanism to the heat exchanger 3 for heat exchange; the second pipeline 11 sends the heat-exchanged gas to the bottom of the riser reactor 1 to participate in the catalytic reaction; the third pipeline 12 is responsible for transporting the reacted gas and catalyst mixture to the catalyst stripping tower 2; the fourth pipeline 13 realizes the reflux of the catalyst from the stripping tower to the lower part of the riser reactor 1; the fifth pipeline 14 ensures that the stripping gas provided by the second gas supply mechanism 6 directly enters the bottom of the catalyst stripping tower 2 to complete the catalyst regeneration process. This pipeline system ensures the smooth operation of the entire production process.

[0055] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a first gas-solid separator 15, a second gas-solid separator 16 and a sixth pipeline 17. The first end of the first gas-solid separator 15 is connected to the riser reactor 1 through the third pipeline 12, and the second end of the first gas-solid separator 15 is connected to the catalyst stripping tower 2. The first end of the second gas-solid separator 16 is connected to the third end of the first gas-solid separator 15, and the second end of the second gas-solid separator 16 is connected to the catalyst stripping tower 2. And one end of the sixth pipeline 17 is connected to the third end of the second gas-solid separator 16, and the other end of the sixth pipeline 17 is connected to the heat exchanger 3.

[0056] Specifically, the first gas-solid separator 15 and the second gas-solid separator 16 together with the sixth pipeline 17 constitute the key link of gas-solid separation and circulation. The gas-solid mixture output from the riser reactor 1 through the third pipeline 12 first enters the first gas-solid separator 15 to achieve preliminary separation, wherein the solid catalyst part continues to enter the catalyst stripping tower 2, and the gas part merges with the further separated gas in the second gas-solid separator 16. Subsequently, the gas purified by the second gas-solid separator 16 returns to the heat exchanger 3 through the sixth pipeline 17 for heat exchange and recycling. This process effectively improves the gas-solid separation efficiency of the system and the recovery rate of the catalyst. Among them, the first gas-solid separator 15 and the second gas-solid separator 16 are both arranged in the upper space of the catalyst stripping tower 2.

[0057] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes: a seventh pipeline 18 and an eighth pipeline 19. One end of the seventh pipeline 18 is connected to the liquid outlet of the liquid supply mechanism 5, and the other end of the seventh pipeline 18 is connected to the lower part of the riser reactor 1. One end of the eighth pipeline 19 is connected to the liquid return port of the liquid supply mechanism 5, and the other end of the eighth pipeline 19 is connected to the upper part of the riser reactor 1.

[0058] Specifically, the seventh pipeline 18 and the eighth pipeline 19 together constitute the key channel of the hot liquid circulation. The seventh pipeline 18 is responsible for transporting the high-temperature hot liquid heated by the liquid supply mechanism 5 to the bottom of the riser reactor 1 to provide the necessary heat energy for the catalytic reaction; while the eighth pipeline 19 realizes the recovery of the hot liquid after the reaction, and leads it back to the liquid supply mechanism 5 from the upper part of the reactor for reheating, forming a closed-loop hot liquid circulation system. This design not only improves the utilization efficiency of thermal energy, but also helps to maintain the stability of the temperature in the reactor, ensuring the continuous and efficient progress of the catalytic reaction.

[0059] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes a ninth pipeline 20, a tenth pipeline 21, an eleventh pipeline 22 and a condensate pump 23. One end of the ninth pipeline 20 is connected to the heat exchanger 3, and the other end of the ninth pipeline 20 is connected to the air cooler 9. One end of the tenth pipeline 21 is connected to the air cooler 9, and the other end of the tenth pipeline 21 is connected to the condensate tank 7. One end of the eleventh pipeline 22 is connected to the condensate tank 7, and the other end of the eleventh pipeline 22 is connected to the liquid supply mechanism 5. And the condensate pump 23 is arranged on the eleventh pipeline 22.

[0060] Specifically, the ninth pipeline 20, the tenth pipeline 21 and the eleventh pipeline 22 work together with the condensate pump 23 to form an important link for condensate recovery and recycling. The high-temperature gas flowing out of the heat exchanger 3 first passes through the ninth pipeline 20 to enter the air cooler 9 for cooling, and then the cooled gas and condensate flow into the condensate tank 7 through the tenth pipeline 21. In the condensate tank 7, the gas is further condensed into liquid, and returns to the liquid supply mechanism 5 for recycling through the eleventh pipeline 22 under the drive of the condensate pump 23. This process not only realizes the efficient recovery of condensate, but also helps to maintain the balance of materials inside the system and improve the overall operating efficiency.

[0061] In a specific embodiment, the first mixed gas and the second mixed gas enter the heat exchanger 3 through the sixth pipeline 17 for heat exchange, and then enter the air cooler 9 to cool to 30°C, condense the water vapor in the mixed gas, enter the condensation tank 7 for separation, and the gas phase is the product synthesis gas and the liquid phase is the condensate. The condensate is pumped into the liquid supply mechanism 5 through the condensate pump 23, and the liquid supply mechanism 5 and the steam generator are integrated. The condensate is heated and gasified in the steam generator of the liquid supply mechanism to obtain water vapor, and the water vapor returns to the first gas supply mechanism 4 and the second gas supply mechanism 6 for recycling.

[0062] In one embodiment of the present invention, the first gas supply mechanism 4 includes: a first gas supply unit 24, a second gas supply unit 25 and a third gas supply unit 26. The first gas supply unit 24 is used to provide methane, and the first gas supply unit 24 is connected to the first pipeline 10 through a twelfth pipeline 33. The second gas supply unit 25 is used to provide carbon dioxide, and the second gas supply unit 25 is connected to the first pipeline 10 through a thirteenth pipeline 34. And the third gas supply unit 26 is used to provide water vapor, and the third gas supply unit 26 is connected to the first pipeline 10 through a fourteenth pipeline 35.

[0063] Specifically, the first gas supply mechanism 4 is a key gas supply mechanism in the photothermal catalytic fluidized reaction system for producing synthesis gas, and it is composed of three independent gas supply units: the first gas supply unit 24 specifically provides methane as one of the reaction gases, and is directly connected to the main gas supply system (first pipeline 10) through the twelfth pipeline 33; the second gas supply unit 25 is responsible for supplying carbon dioxide, and is also connected to the main system (first pipeline 10) through the thirteenth pipeline 34; and the function of the third gas supply unit 26 is to provide water vapor, and it uses the fourteenth pipeline 35 to introduce water vapor into the main gas supply pipeline (first pipeline 10). These three gas supply units work together to ensure the stable supply and precise proportion of the gas required for the reaction.

[0064] In one embodiment of the present invention, the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction further includes a control mechanism, a first flow control valve 27, a second flow control valve 28, a third flow control valve 29, a fourth flow control valve 30, a first electronic valve 31 and a second electronic valve 32. The first flow control valve 27 is arranged on the twelfth pipeline 33, and the first flow control valve 27 is electrically connected to the control mechanism. The second flow control valve 28 is arranged on the thirteenth pipeline 34, and the second flow control valve 28 is electrically connected to the control mechanism. The third flow control valve 29 is arranged on the fourteenth pipeline 35, and the third flow control valve 29 is electrically connected to the control mechanism. The fourth flow control valve 30 is arranged on the fifth pipeline 14, and the fourth flow control valve 30 is electrically connected to the control mechanism. The first electronic valve 31 is arranged on the seventh pipeline 18, and the first electronic valve 31 is electrically connected to the control mechanism. And the second electronic valve 32 is disposed on the eighth pipe 19 , and the second electronic valve 32 is electrically connected to the control mechanism.

[0065] Specifically, the present invention integrates an advanced automatic control mechanism, and realizes fine control of the entire production process through precisely arranged flow control valves and electronic valves. The control mechanism is electrically connected to each flow control valve (respectively located on the twelfth pipeline 33, the thirteenth pipeline 34, the fourteenth pipeline 35 and the fifth pipeline 14) and the electronic valve (arranged on the seventh pipeline 18 and the eighth pipeline 19), and can monitor and adjust the flow of gas and liquid in real time to ensure the stability and optimality of the reaction conditions. This highly automated control system not only improves production efficiency and product quality, but also greatly reduces the burden on operators.

[0066] In a specific embodiment of the present invention, the working process of the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in actual application is as follows:

[0067] 1. The reaction raw materials of carbon dioxide, methane and water vapor (i.e., the first gas is introduced from the public engineering system, i.e., provided by the first gas supply mechanism 4) are mixed through flow control (i.e., controlled by the first flow control valve 27, the second flow control valve 28 and the third flow control valve 29), heat exchanged with the heat exchanger 3, and injected into the bottom of the riser reactor 1. The steam ratio in the raw materials can be increased and decreased according to the product H2 / CO ratio requirements. The first gas and the catalyst are contacted with the gas distributor and the catalyst inside the riser reactor 1, and a catalytic reaction is carried out in the riser reactor 1 to produce a mixed gas of hydrogen and carbon monoxide (i.e., a first mixed gas is obtained).

[0068] 2. Solar thermal energy is introduced into the molten salt device through high-temperature concentrating technology (i.e., solar thermal energy is introduced into the liquid supply mechanism 5 through the high-temperature concentrating mechanism 8 and the light-transmitting mirror), and the molten salt is heated to 700°C (i.e., there is molten salt in the liquid supply mechanism 5). Part of the heated molten salt is used to supply heat (hot liquid) to the riser reactor 1, part is used to produce steam, and the other part is used to store heat, which provides heat for the device at night or when there is no sunlight, ensuring continuous production of the device.

[0069] 3. Open the connecting valves between the molten salt device and the riser reactor 1 (i.e., the first electronic valve 31 and the second electronic valve 32) to ensure that the molten salt (hot liquid) circulates continuously between the two devices. The outlet temperature of the riser reactor 1 is controlled in the range of 600-680°C.

[0070] 4. The catalyst is a transition element metal including (but not limited to) nickel, palladium, iridium, platinum, ruthenium, rhodium, etc. or their alloys, and the carrier is a metal oxide including (but not limited to) cerium dioxide or aluminum oxide, etc. The catalyst formula is designed to achieve the maximum conversion rate of the first gas, and the reforming chemical reaction is carried out with the first gas in the riser reactor 1. The reaction balance in the riser reactor 1 is:

[0071] 1) The feed does not contain water vapor

[0072]

[0073] 2) The feed contains water vapor

[0074]

[0075] 5. The outlet gas of the riser reactor 1 is a mixed gas of hydrogen and carbon monoxide (first mixed gas), which is separated by the first gas-solid separator 15 outside the riser reactor 1. The separated catalyst solid passes through the catalyst stripping tower 2 and steam to clean the carbon deposit on the catalyst surface and replace the synthesis gas entrained between the particles, and then returns to the riser reactor 1 through the inclined pipe (fourth pipeline 13) connecting the catalyst stripping tower 2 and the riser reactor 1 for reaction. The slide valve 37 on the fourth pipeline 13 (electrically connected to the control mechanism) is used to control the catalyst flow rate. The mass flow ratio of the catalyst and the raw material is about 8 to 12, and the separated gas is discharged from the top. Among them, all the heat required for the reaction actually comes from the molten salt. The molten salt heats the circulating catalyst, and the catalyst transfers heat to the reactants to complete the reaction process. Therefore, indirectly, the reaction temperature is controlled by the catalyst circulation amount, that is, by the slide valve 37 provided on the catalyst tube. The heat of the molten salt is large enough and is not controlled. The outlet of the riser is provided with a reaction temperature detection instrument, and the output value of the temperature and the given value of the reaction temperature automatically controls the opening of the slide valve 37, thereby achieving the purpose of stable control of the reaction temperature. In actual applications, the catalyst is mixed with the material in the second pipeline 11 through the fourth pipeline 13, and the temperature is about 600°C, and enters the inner ring of the riser reactor 1. The 700°C molten salt enters the outer ring of the sleeve riser reactor 1 through the seventh pipeline 18 to heat the material. After the temperature of the inner ring of the riser reactor 1 is heated to 680°C, it enters the first gas-solid separator 15, and the 690°C molten salt enters the subsequent storage tank through the eighth pipeline 19. Among them, Figure 1 and Figure 4 As shown by the middle dotted line, the catalyst inventory control of the reactor is controlled by the slide valve 37 (or plug valve) on the catalyst delivery pipe, that is, the slide valve 37 on the catalyst pipe normally controls the reaction temperature, and the catalyst inventory of the reactor is tracked as a secondary control target. If the reactor inventory exceeds the maximum value, it switches to the slide valve to control the inventory. The reaction temperature becomes a secondary control parameter at this time, and the reactor is equipped with a catalyst inventory detection instrument, which does not participate in the control under normal circumstances. Among them, Figure 1 and Figure 4 The WIC in it stands for volume control and TIC stands for temperature control.

[0076] 6. The catalyst contacts CH4 and CO2 in the riser reactor 1 to undergo a reforming reaction to produce synthesis gas (CO+H2). A small amount of steam is added to optimize the composition of the synthesis gas product, and the feed CO2:CH4:H2O ratio is about 1:2:1. No CO2 appears during the synthesis gas production process, and a small amount of residual carbon is formed on the catalyst surface. After contacting with steam in the catalyst stripper 2, the catalyst is completely regenerated.

[0077] 7. Stripping steam is injected into the bottom of the catalyst stripping tower 2 (i.e., the second gas is provided by the second gas supply mechanism 6) to strip the catalyst. The gas at the outlet of the stripping tower is separated by the second gas-solid separator 16. The separated solid returns to the catalyst stripping tower 2. The separated gas contains a small amount of hydrogen and carbon monoxide and is mixed with the gas separated by the first gas-solid separator 15 outside the riser reactor 1 (i.e., the first mixed gas and the second mixed gas are mixed). The mixed gas is cooled by the heat exchanger 3, and then cooled to 30°C by the air cooler 9, and finally enters the condenser 7. The product synthesis gas is discharged from the top of the condenser 7. The condensed water recovered at the bottom of the condenser 7 and the supplemented desalted water enter the molten salt device together to generate low-pressure steam for the device to circulate.

[0078] 8. By adjusting the amount of carbon dioxide blended, the composition ratio of hydrogen and carbon monoxide in the synthesis gas product is increased or decreased, and the molar ratio of synthesis gas H2:CO is approximately in the range of 1 to 2:1, which is suitable for supplying raw materials to Fischer-Tropsch synthesis plants and producing sustainable renewable jet fuel SAF.

[0079] 9. Typical physical and chemical properties of catalysts

[0080] project nature Remark <![CDATA[Heap ratio, kg / m 3 > 800-1000 <![CDATA[Specific surface area, m 2 / g]]> 200-250 Wear resistance index ＜3 Average particle size, μm 100-200

[0081] 10. Design case product yield

[0082] 1) Syngas composition ratio H2:CO 1:1

[0083] Syngas product flow rate 13393kg / h

[0084] Raw material flow CO2 9821kg / h

[0085] CH4 3571kg / h

[0086] Solar thermal input 17MW

[0087] Energy efficiency>80%.

[0088] 2) The feed contains water vapor

[0089] Syngas composition ratio H2:CO 2:1

[0090] Syngas product flow rate 9524kg / h

[0091] Raw material flow rate H2O 2679kg / h

[0092] CO2 3274kg / h

[0093] CH4 3571kg / h

[0094] Solar thermal input 15MW

[0095] Energy efficiency>80%.

[0096] 3) Optimize water vapor in the feed

[0097] Syngas composition ratio H2:CO 1.7:1

[0098] Syngas product flow rate 10491kg / h

[0099] Raw material flow rate H2O 2009kg / h

[0100] CO2 4911kg / h

[0101] CH4 3571kg / h

[0102] Solar thermal input 16MW

[0103] Energy efficiency>80%.

[0104] The present invention can also set up a SIS system, including hardware and software. The measured values ​​of the relevant interlocking items are introduced into the SIS and compared with the set interlocking values. If the interlocking values ​​are reached, the valve shutdown operation is implemented according to the interlocking logic to protect the equipment. Among them, the main items of the trigger device for safety protection of the SIS are: high reaction pressure: such as 1.0MPaG; high reaction temperature: such as 700°C; low feed flow rate: such as 50% feed volume; molten salt supply interruption. By setting up the SIS system, it can be ensured that a rapid response and safe shutdown can be achieved in abnormal situations.

[0105] Embodiment 2

[0106] Figure 3 : is a schematic flow diagram of a method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Example 2 of the present invention, such as Figure 3 As shown, Example 2 provides a method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction. Based on the above-mentioned system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, the method includes:

[0107] Step S100, adding a first gas into the riser reactor to fluidize the catalyst in the riser reactor;

[0108] Step S200, providing hot liquid to the riser reactor through a liquid supply mechanism for heating, so that the fluidized catalyst and the first gas undergo a chemical reaction to obtain a reacted catalyst and a first mixed gas;

[0109] Step S300, transporting the reacted catalyst to a catalyst stripping tower, and adding a second gas to the catalyst stripping tower, thereby stripping and cleaning the carbon deposits on the surface of the reacted catalyst to obtain a catalyst and a second mixed gas;

[0110] Step S400, transporting the catalyst in the catalyst stripping tower to the riser reactor;

[0111] Step S500: Mix the first mixed gas and the second mixed gas, and transport them to a condensation tank to generate synthesis gas.

[0112] The various variations and specific examples of the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction provided in Example 1 are also applicable to the method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction provided in this embodiment. Through the above detailed description of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, those skilled in the art can clearly know the implementation method of the method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in this embodiment, so for the sake of brevity of the specification, it will not be described in detail here.

[0113] Embodiment 3

[0114] Figure 4 FIG. 1 is a schematic diagram of a part of a system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction in Embodiment 3 of the present invention. Figure 4 As shown, the riser reactor 1 in Example 3 is an inner riser reactor, while the riser reactor 1 in Example 1 is an outer riser reactor. The inner riser reactor and the outer riser reactor have the same working principle, that is, the difference between Example 3 and Example 1 is only the implementation method of the riser reactor. The outer riser reactor is entirely a pressure vessel, and all require a heat-insulating and wear-resistant lining; while the inner riser reactor has only the components outside the reactor that are pressure vessels, which require a heat-insulating and wear-resistant lining, and the portion extending into the catalyst stripping tower and above the stripping section is only provided with a wear-resistant lining in the inner riser reactor, and no insulation is required. Among them, the outer riser reactor is as follows: Figure 1 As shown, the inner riser reactor is as Figure 4 As shown, a portion extends into the catalyst stripping tower. The stripping section of the catalyst stripping tower is the portion with grid packing ( Figure 4 the position of the cross pattern in the middle).

[0115] In summary, the system and method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction of the present invention are low-carbon and environmentally friendly. They utilize green energy carbon capture technology (Carbon Capture & Utilization, CCU Technology) to industrially recover and utilize carbon dioxide, utilize solar energy photothermal energy to efficiently provide energy, and react with methane in bio-recovered fuel gas or natural gas to produce synthesis gas, which can be used to produce green or blue methanol, and produce low-carbon olefins through MTO (Methanol to Olefin) technology. In addition, the synthesis gas can also be used to produce low-carbon transportation fuels, including sustainable aviation kerosene (SAF), and improve energy utilization efficiency.

[0116] Note that the above are only preferred embodiments of the present invention and the technical principles used. Those skilled in the art will understand that the present invention is not limited to the specific embodiments described herein, and that various obvious changes, readjustments and substitutions can be made by those skilled in the art without departing from the scope of protection of the present invention. Therefore, although the present invention has been described in more detail through the above embodiments, the present invention is not limited to the above embodiments, and may include more other equivalent embodiments without departing from the concept of the present invention, and the scope of the present invention is determined by the scope of the appended claims.

Claims

1. A system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, using carbon dioxide and methane as raw materials, characterized in that: The system comprises: A riser reactor having a catalyst therein, and the riser reactor is used for a chemical reaction of reforming carbon dioxide and methane to obtain a post-reaction catalyst and a first mixed gas; A catalyst stripping tower is connected to the riser reactor and is used to strip and clean carbon deposits on the surface of the catalyst after the reaction to obtain the catalyst and the second mixed gas; a heat exchanger connected to the riser reactor; a first gas supply mechanism connected to the heat exchanger, and used to provide a first gas to the riser reactor through the heat exchanger, so as to perform a catalytic reaction with the catalyst; a liquid supply mechanism connected to the riser reactor and used to provide hot liquid to the riser reactor; a second gas supply mechanism connected to the catalyst stripping tower, and the second gas supply mechanism is used to provide a second gas to the catalyst stripping tower, and the second gas is used to strip the reacted catalyst; and A condensation tank, one end of which is connected to the heat exchanger, and the other end of which is connected to the liquid supply mechanism, and the condensation tank is used to receive the first mixed gas and the second mixed gas to generate synthesis gas.

2. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 1, characterized in that: Also includes: A high-temperature focusing mechanism, used to provide solar heat, and located above the liquid supply mechanism; as well as A light-transmitting mirror is arranged on the top of the liquid supply mechanism, and is used to receive the solar heat provided by the high-temperature focusing mechanism and introduce the solar heat into the liquid supply mechanism, thereby heating the molten salt in the liquid supply mechanism to form the hot liquid.

3. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 1, characterized in that: It also includes an air cooler, one end of which is connected to the heat exchanger, and the other end of which is connected to the condensing tank.

4. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 1, characterized in that: Also includes: a first pipeline, one end of which is connected to the first air supply mechanism, and the other end of which is connected to the heat exchanger; a second pipeline, one end of which is connected to the heat exchanger and the other end of which is connected to the bottom of the riser reactor; a third pipeline, one end of which is connected to the upper portion of the riser reactor, and the other end of which is connected to the catalyst stripping tower; a fourth pipeline, one end of which is connected to the bottom of the catalyst stripping tower, and the other end of which is connected to the lower portion of the riser reactor; and A fifth pipeline, one end of which is connected to the second gas supply mechanism, and the other end of which is connected to the lower part of the catalyst stripping tower.

5. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 4, characterized in that: Also includes: a first gas-solid separator, wherein a first end of the first gas-solid separator is connected to the riser reactor through the third pipeline, and a second end of the first gas-solid separator is connected to the catalyst stripping tower; a second gas-solid separator, wherein a first end of the second gas-solid separator is connected to a third end of the first gas-solid separator, and a second end of the second gas-solid separator is connected to the catalyst stripping tower; and A sixth pipeline, one end of the sixth pipeline is connected to the third end of the second gas-solid separator, and the other end of the sixth pipeline is connected to the heat exchanger.

6. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 4, characterized in that: Also includes: a seventh pipeline, one end of which is connected to the liquid outlet of the liquid supply mechanism, and the other end of which is connected to the lower part of the riser reactor; as well as An eighth pipeline, one end of which is connected to the liquid return port of the liquid supply mechanism, and the other end of which is connected to the upper part of the riser reactor.

7. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction as claimed in claim 3, characterized in that: Also includes: a ninth pipeline, one end of which is connected to the heat exchanger, and the other end of which is connected to the air cooler; a tenth pipeline, one end of which is connected to the air cooler, and the other end of which is connected to the condensing tank; an eleventh pipeline, one end of the eleventh pipeline being connected to the condensing tank, and the other end of the eleventh pipeline being connected to the liquid supply mechanism; and The condensate pump is arranged on the eleventh pipeline.

8. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 6, characterized in that: The first air supply mechanism comprises: a first gas supply unit, used for providing methane, and the first gas supply unit is connected to the first pipeline through a twelfth pipeline; a second gas supply unit, configured to provide carbon dioxide, wherein the second gas supply unit is connected to the first pipeline via a thirteenth pipeline; and The third gas supply unit is used to provide water vapor, and the third gas supply unit is connected to the first pipeline through a fourteenth pipeline.

9. The system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction according to claim 8, characterized in that: Also includes: Controlling bodies; a first flow control valve, disposed on the twelfth pipeline, and the first flow control valve is electrically connected to the control mechanism; a second flow control valve, disposed on the thirteenth pipeline, and the second flow control valve is electrically connected to the control mechanism; a third flow control valve, disposed on the fourteenth pipeline, and the third flow control valve is electrically connected to the control mechanism; a fourth flow control valve, disposed on the fifth pipeline, and the fourth flow control valve is electrically connected to the control mechanism; a first electronic valve, disposed on the seventh pipeline, and the first electronic valve is electrically connected to the control mechanism; and The second electronic valve is disposed on the eighth pipeline, and the second electronic valve is electrically connected to the control mechanism.

10. A method for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction, based on the system for producing synthesis gas by photothermal catalytic fluidized carbon capture reaction as claimed in any one of claims 1 to 9, characterized in that: The method comprises: adding a first gas into the riser reactor to fluidize the catalyst in the riser reactor; supplying hot liquid to the riser reactor through a liquid supply mechanism to supply heat, so that the fluidized catalyst reacts chemically with the first gas to obtain a reacted catalyst and a first mixed gas; The post-reaction catalyst is transported to a catalyst stripping tower, and a second gas is added to the catalyst stripping tower, so as to strip and clean the carbon deposits on the surface of the post-reaction catalyst to obtain a catalyst and a second mixed gas; transporting the catalyst in the catalyst stripping tower to the riser reactor; The first mixed gas and the second mixed gas are mixed and transported to a condensation tank to generate synthesis gas.

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