Device for preparing methanol by hydrogenating carbon dioxide in combination with chemical looping combustion and preparation method thereof

Abstract

The invention belongs to the technical field of methanol preparation, and particularly relates to a device for preparing methanol through carbon dioxide hydrogenation in combination with chemical looping combustion and a preparation method.The device comprises a power generation system, an electrolytic tank, a chemical looping combustion reactor, a pure oxygen afterburning chamber and a methanol reaction unit, oxygen generated by electrolysis of the electrolytic tank is connected with the chemical-looping combustion reactor through a first pipeline, the oxygen generated by electrolysis of the electrolytic tank is connected with the pure oxygen afterburning chamber through a second pipeline, the chemical-looping combustion reactor is connected with a raw material pipeline, and the top of the chemical-looping combustion reactor is connected with the pure oxygen afterburning chamber through a third pipeline. The pure oxygen afterburning chamber is connected with the methanol reaction unit through a fourth pipeline, hydrogen generated by electrolysis of the electrolytic tank is connected with the methanol reaction unit through a fifth pipeline, and a reaction product is discharged through a sixth pipeline.

Description

Technical Field

[0001] The present invention belongs to the technical field of methanol preparation, and specifically relates to a device and a preparation method for preparing methanol by hydrogenating carbon dioxide combined with chemical chain combustion. Background Art

[0002] Methanol is an important chemical product, a raw material for a variety of high-value-added chemicals, and an important solvent in organic chemistry. As the most widely used basic chemical raw material and high-quality fuel, methanol can not only be used to prepare chemicals such as aromatics and olefins, but can also be directly used as fuel for fuel cells. Methanol plays an important role in the pharmaceutical, fuel, plastic, synthetic fiber and other industries. Karolubia, a Nobel Prize winner in physics, has repeatedly proposed the use of carbon dioxide hydrogenation to produce methanol to achieve carbon dioxide emission reduction and provide industrial basic raw materials. Another Nobel Prize winner, George Andrew Euler, proposed in his book that the cycle mode of renewable energy hydrogen production and carbon dioxide hydrogenation to produce methanol is a way to solve the energy shortage problem after the oil and gas era. By coupling carbon dioxide capture technology with green hydrogen production technology, industrial hard-emission carbon dioxide can be recycled. Large-scale green methanol can not only be used directly or indirectly as fuel to alleviate China's shortage of liquid fuels; it can also be used as a hydrogen carrier to solve the safety and cost problems of hydrogen energy preparation, storage and transportation, and provide a feasible technical route for solving the large-scale storage and peak load balancing problems of intermittent energy such as wind energy and solar energy, connecting the carbon-neutral green economic ecological chain of multiple industries.

[0003] However, there are some problems in the current process of producing methanol by hydrogenation of carbon dioxide. First, in the current production process, there is no reasonable disposal method for the pure oxygen obtained in the process of producing hydrogen by electrolysis of water; on the other hand, in order to achieve the purpose of emission reduction, the carbon dioxide used as raw material is often the tail gas of fossil fuel combustion, and the tail gas of conventional combustion contains a large amount of nitrogen, which dilutes the carbon dioxide, making the purity of the carbon dioxide in the combustion tail gas unable to meet the requirements of subsequent process value-added utilization, and it is necessary to add a complex and difficult step of separating nitrogen and carbon dioxide. At the same time, the energy waste and pollutant emissions caused by conventional combustion methods are also contrary to the purpose of using carbon dioxide hydrogenation to produce methanol. Summary of the invention

[0004] In view of the above defects of the existing methods, the present invention provides a device and preparation method for producing methanol by hydrogenating carbon dioxide combined with chemical chain combustion, which solves the technical problems of low purity, complex process and environmental unfriendliness of methanol preparation in the prior art.

[0005] According to a first aspect of the present invention, there is provided a device for producing methanol by hydrogenating carbon dioxide in combination with chemical looping combustion, comprising a power generation system, an electrolytic cell, a chemical looping combustion reactor, a pure oxygen afterburner, and a methanol reaction unit, wherein the power generation system is connected to the electrolytic cell, the electrolytic cell is connected to the chemical looping combustion reactor via a first pipeline, the electrolytic cell is connected to the pure oxygen afterburner via a second pipeline, the chemical looping combustion reactor is connected to a raw material pipeline, the top of the chemical looping combustion reactor is connected to the pure oxygen afterburner via a third pipeline, the pure oxygen afterburner is connected to the methanol reaction unit via a fourth pipeline, the hydrogen generated by electrolysis in the electrolytic cell is connected to the methanol reaction unit via a fifth pipeline, and the methanol reaction unit is connected to a sixth pipeline.

[0006] Preferably, the chemical chain combustion reactor includes a fuel reactor, a first cyclone separator, a second cyclone separator, an air reactor, a first flow sealing valve, and a second flow sealing valve; the fuel reactor is connected to the first pipeline, the top of the fuel reactor is connected to the top of the air reactor through the first cyclone separator, and the top of the fuel reactor is also connected to the top of the pure oxygen afterburning chamber through the second cyclone separator; the bottom of the fuel reactor is connected to the bottom of the air reactor through the first flow sealing valve, and the bottom of the fuel reactor is also connected to the bottom of the second cyclone separator through the second flow sealing valve, the top of the air reactor is connected to the seventh pipeline, the bottom of the air reactor is connected to the air pipeline, and the top of the second cyclone separator is connected to the third pipeline.

[0007] Preferably, the fourth pipeline is connected to a condenser, and the condenser is connected to the electrolytic cell through an eighth pipeline.

[0008] Preferably, the methanol reaction unit is specifically: a first heat exchanger, a fixed bed reactor, a first flash kettle, a second flash kettle, a fractionator, and a third flash kettle are connected in sequence, the second pipeline is connected to the fourth pipeline and the ninth pipeline, the ninth pipeline is connected to the first heat exchanger, the tops of the first flash kettle, the second flash kettle, and the third flash kettle are connected to the ninth pipeline through the tenth pipeline, the eleventh pipeline, and the twelfth pipeline respectively, and the first heat exchanger is connected to the seventh pipeline.

[0009] Preferably, the raw material pipeline is used to introduce biomass, and the fuel reactor is loaded with an oxygen carrier, and the oxygen carrier is selected from one or more of Fe2O3, CuO, NiO, Mn2O3, CaSO4, BaSO4, CaFe2O5, CuFe2O4, and perovskite; the biomass is selected from one or more of sawdust, straw, and rice husk.

[0010] Preferably, the pure oxygen afterburner is filled with a mixture of a single substance or compound containing precious metals or non-precious metal elements and Fe2O3, CuO, NiO, Mn2O3, CO3O4, or perovskite as a catalyst, and the precious metal is selected from Ag, Pd, Pt, Au, Rh, and Ir; the non-precious metal is selected from Mn, Ce, and Sr; the fixed bed reactor is filled with a methanol synthesis catalyst, and the methanol synthesis catalyst is selected from one or more of Cu and Pd.

[0011] According to another aspect of the present invention, there is provided a method for preparing methanol from a device for preparing methanol from carbon dioxide hydrogenated by chemical looping combustion, comprising the following steps:

[0012] (1) supplying power to an electrolytic cell through a power generation system, and the electrolytic cell electrolyzes water to produce hydrogen and oxygen;

[0013] (2) introducing biomass, oxygen carrier, and oxygen produced by electrolyzed water with a volume fraction of 80 to 90% into the bottom of a chemical looping combustion reactor;

[0014] (3) introducing the gas generated after the reaction in step (2) together with oxygen generated by electrolysis of water with a volume fraction of 10 to 20% into a pure oxygen afterburner, and further reacting under the action of a catalyst to completely convert the biomass into carbon dioxide gas;

[0015] (4) The carbon dioxide and hydrogen obtained by electrolysis of water are combined to form a raw gas, and the raw gas is introduced into a methanol reaction unit to obtain methanol.

[0016] Preferably, step (2) is specifically as follows: biomass is introduced into a fuel reactor containing an oxygen carrier for reaction, the gas generated by the reaction is separated into gas and solid by a second cyclone separator, the separated gas phase is introduced into a pure oxygen afterburning chamber for further reaction, the separated solid phase is returned to the fuel reactor through a second flow sealing valve, the oxygen carrier at the bottom of the fuel reactor enters the bottom of the air reactor through a first flow sealing valve, and after being fully mixed with the air introduced into the air reactor, enters the first cyclone separator for gas and solid separation, the separated solid is the oxidized oxygen carrier, which falls into the fuel reactor to achieve circulation.

[0017] Preferably, step (4) is specifically the following: the feed gas is passed into a first heat exchanger, the air reactor tail gas generated in the air reactor is heat exchanged with the feed gas in the first heat exchanger to heat the feed gas, and the feed gas temperature is maintained at 200-300°C, the heated feed gas is sequentially passed into a fixed bed reactor, a first flash kettle, a second flash kettle, a fractionator, and a third flash kettle for sufficient reaction, the third flash kettle flashes to produce a liquid product, methanol, and the gaseous product produced by the reaction of the first flash kettle, the second flash kettle, and the third flash kettle is returned to the feed gas for further sufficient reaction.

[0018] Preferably, the carbon dioxide gas produced in step (3) is condensed through a condenser, and the produced condensed water is passed into the electrolytic cell.

[0019] In general, the above technical solution conceived by the present invention has the following technical advantages compared with the prior art:

[0020] 1. The present invention uses a chemical chain combustion method to burn biomass to obtain carbon dioxide, avoiding direct contact between air and biomass, so that biomass can be directly converted into high-concentration carbon dioxide without being affected by nitrogen dilution, thereby making the prepared methanol high in purity and free of by-products such as nitrogen oxides and sulfur oxides.

[0021] 2. The present invention adopts a chemical chain combustion reactor to oxidize biomass. After the biomass is oxidized, there will generally be certain sulfur oxides and nitrogen oxides. However, in chemical chain combustion, firstly, the distribution of temperature and components is more uniform, and the unique low O2 and reducing atmosphere helps to reduce most of the fuel nitrogen to N2, and the temperature reduction can inhibit the rapid and thermal NO x The SO generated can be removed in situ by CaO etc. x , so the sulfur oxides and nitrogen oxides in chemical looping combustion are significantly lower.

[0022] 3. The present invention adopts oxygen carrier, taking Fe2O3 as an example, which contains O 2- It is called lattice oxygen. Fe2O3 is reduced to a lower valence state Fe3O4 during the reaction with the fuel gas in the fuel reactor. In this process, the lattice oxygen is consumed and the oxygen carrier is reduced. After the oxygen carrier is reduced, it enters the air reactor. The air reactor and the fuel reactor are separated by a cyclone separator and a flow sealing valve. There is only the exchange of oxygen carriers and basically no exchange of gas. In the air reactor, the oxygen carrier reacts with the air passing through it, and FeO is reoxidized to Fe3O4, and the lattice oxygen is replenished. The oxygen carrier with replenished lattice oxygen returns to the fuel reactor to continue to react with the fuel gas to provide lattice oxygen. In this way, from a macroscopic point of view, the metal oxide plays the role of converting the gas phase oxygen in the air into lattice oxygen, and then transporting it to the fuel reactor for recycling.

[0023] 4. The methanol reaction device of the present invention utilizes the advantages of triple flash evaporation technology. When using a relatively cheap and inefficient catalyst, it can effectively separate the gas phase components containing incompletely reacted raw gas and by-products, and enrich the liquid phase components containing methanol. By reintroducing the gas phase products into the reactor for reaction, CO2, CO and H2 in the gas phase products will continuously react in the circulation loop, thereby improving the utilization rate of raw materials and reducing the generation of by-products, thereby making the carbon dioxide conversion rate and methanol selectivity in the overall process flow exceed 99%.

[0024] 5. The present invention utilizes pure oxygen obtained by electrolyzing water to further convert the tail gas of chemical chain combustion in a pure oxygen afterburner, thereby realizing the utilization of pure oxygen. Meanwhile, the biomass is completely converted into carbon dioxide after re-oxidation, and the water vapor in the carbon dioxide is condensed into water to obtain high-purity carbon dioxide gas, which can be used as a raw material for preparing methanol. Meanwhile, the water obtained by condensing the water vapor is added to the electrolytic cell as a raw material, thereby realizing the circulation of logistics and improving the utilization rate. The present invention utilizes the high-temperature flue gas generated in the chemical chain combustion process as a heat source, and heat-exchanges and heats the hydrogen and carbon dioxide raw gas through a first heat exchanger to maintain the temperature of the carbon dioxide hydrogenation system to realize the effective utilization of thermal energy.

[0025] 6. The entire method of the present invention only requires biomass and green electricity as the input carbon sources to obtain green methanol. Multiple subsystems including electrolytic cell, chemical chain combustion, and carbon dioxide hydrogenation to produce methanol are integrated to form a stable and feasible energy flow cycle, achieving multi-subsystem coupling, high-efficiency, and negative-carbon methanol preparation, realizing the resource utilization of waste, and at the same time, no other waste gas is generated. Therefore, the methanol preparation method of the present invention is completely green. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic diagram of the process system for producing methanol from carbon dioxide hydrogenation combined with chemical looping combustion of the present invention.

[0027] Figure 2 Schematic diagram of the methanol reaction unit of the present invention.

[0028] Figure 3 It is the yield of each component of the exhaust gas from the biomass chemical chain combustion reactor of the present invention.

[0029] Figure 4 It is the conversion rate of each component of the exhaust gas from the pure oxygen afterburner of the present invention.

[0030] In the figure, 1, power generation system; 2, electrolytic cell; 3, chemical chain combustion reactor; 4, pure oxygen afterburner; 5, methanol reaction unit; 6, condenser; 101, first pipeline; 102, fifth pipeline; 111, second pipeline; 104, raw material pipeline; 105, third pipeline; 106, air pipeline; 107, seventh pipeline; 108, eighth pipeline; 109, fourth pipeline; 110, sixth pipeline; 31, fuel reactor; 32, first cyclone separator; 33, air reactor; 34, first flow sealing valve; 35, second cyclone separator; 36, second flow sealing valve; 5A, first heat exchanger; 5B, fixed bed reactor; 5C, first flash kettle; 5D, second flash kettle; 5E, fractionator; 5F, third flash kettle; 501, ninth pipeline; 502, tenth pipeline; 503 eleventh pipeline; 504 twelfth pipeline. DETAILED DESCRIPTION

[0031] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention. In addition, the technical features involved in the various embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0032] Example 1

[0033] See also Figure 1 and Figure 2 , a process system for producing methanol from carbon dioxide hydrogenation combined with chemical loop combustion, specifically comprising

[0034] Solar panel 1 is used as a photovoltaic power generation system, which is kept at 25℃ and 1000W / m 2 Under the sunlight radiation intensity, it outputs 7V, 20A DC.

[0035] The photovoltaic power generation system outputs direct current and is fed into the proton exchange membrane electrolyzer 2. The electrolyzer uses a proton exchange membrane to electrolyze water to produce hydrogen and oxygen. The electrolyzer uses precious metals as catalysts. The size of the catalyst of a single electrolyzer is 40*50mm, the hydrogen production is 350mL / min, and the oxygen production is 175mL / min. The purity of the gas obtained by electrolysis is higher than 99.99%. Multiple electrolyzers are integrated to achieve large-scale hydrogen and oxygen production.

[0036] The chemical chain combustion reactor 3 adopts a circulating fluidized bed reactor. The fuel reactor 31 is in a bubbling fluidized bed state, which is filled with Fe2O3. The 90%vol pure oxygen obtained by electrolyzing water is introduced into the fuel reactor 31 from the bottom through the first pipeline 101. The fuel reactor 31 is continuously replenished with biomass particles through the raw material pipeline 104. In the fuel reactor 31, the large amount of sensible heat carried by the oxygen carrier from the air reactor and the reaction heat in the fuel reactor raise the reactor temperature to 950°C. The biomass particles first react with the pure oxygen introduced by the first pipeline 101 to produce fuel gas, and then undergo redox reaction with the oxygen carrier filled in the fuel reactor.

[0037] A first cyclone separator 32 is provided on the upper part of the fuel reactor 31. The reaction products in the fuel reactor 31 enter the first cyclone separator 32 for gas-solid separation. The separated solid phase component is the Fe3O4 oxygen carrier in a reduced state, which falls into the second flow sealing valve 36. The separated fuel reaction gas tail gas is discharged from the third pipeline 105. The CO2 yield of the chemical chain combustion outside the removal of a small amount of escaped particles and water reaches 98.0%, while showing lower CO (0.8%) and CH4 yields (1.2%). The carbon capture efficiency is maintained at 98%, and the combustion efficiency of biomass reaches 95.5%. The results are as follows Figure 3 shown.

[0038] The air reactor 33 is in a fast fluidized bed state. The reduced oxygen carrier at the bottom of the fuel reactor 31 returns to the bottom of the air reactor 33 through the first flow sealing valve 34, and air is introduced through the air pipeline 106. The air oxidizes the reduced oxygen carrier to an oxidized state, and a large amount of heat is released in the process. The oxidized oxygen carrier enters the first cyclone separator 32, and after gas-solid separation, it re-enters the fuel reactor 31 at a mass flow rate of 38.5 kg / s to achieve the circulation of the oxygen carrier. There is only exchange of oxygen carriers but no exchange of gas in the first flow sealing valve 34. A large amount of heat is released in the air reactor 33, and the air reactor tail gas with a temperature of 1000°C is discharged through the seventh pipeline 107 after gas-solid separation in the air reactor 33.

[0039] The filling medium of the pure oxygen afterburner 4 is 500g of Fe2O3 catalyst modified by SrTiO3. The tail gas of the fuel reactor is introduced into the pure oxygen afterburner 4 through the third pipeline 105. At the same time, 10%vol of pure oxygen obtained by electrolyzing water is added to the pure oxygen afterburner 4 through the second pipeline 111. At a temperature of 1050°C, it is fully burned under the action of the catalyst. After the outlet gas is condensed, CO2 with a purity of more than 99% is obtained and discharged through the fourth pipeline 109. The condensed water is introduced into the electrolytic cell 2 through the eighth pipeline 108 for recycling. Under the long-term experiment (more than 10800s) with a reaction temperature of 800°C and an air-fuel ratio of 1.1, the CO conversion rate in the stably operated pure oxygen afterburner 4 is 98.4%, the CH4 conversion rate is 99.4%, the H2 conversion rate is 100%, and the combustion efficiency reaches 99.2%. After removing water vapor and N2 for balance, the proportion of CO2 at the outlet of the deoxygenated afterburner is 99.9%. Figure 4 As shown in the figure, the experimental results prove that at 800°C, when 10% pure oxygen is input into the electrolyzed water, the pure oxygen afterburner can achieve complete conversion of unburned gas in chemical chain combustion to obtain CO2 with a concentration of more than 99.9%. It can be used as a raw material for hydrogenation of carbon dioxide to produce methanol.

[0040] High-purity CO2 enters the ninth pipeline 501 through the fourth pipeline 109 and H2 enters the fifth pipeline 102 to obtain a mixed gas. The mixed gas enters the first heat exchanger 5A through the ninth pipeline 501, is preheated to 250°C by the tail gas of the air reactor discharged from the seventh pipeline 107, and is passed into the fixed bed reactor 5B equipped with a Cu catalyst for reaction. After the reaction, the gas is separated into liquid and vapor products by the first flash reactor 5C, and the liquid product enters the second flash reactor 5D, and is flashed and separated into liquid and vapor products again. The vapor products separated by the first and second flash distillations are collected and mixed with the raw gas, enter the first heat exchanger 5A through the ninth pipeline 501, and are preheated again, and then passed into the fixed bed reactor 5B for recycling. The liquid product produced by the second flash kettle 5D contains unreacted CO2, H2 and by-product CO, which enters the fractionator 5E for distillation. The liquid product obtained by distillation is methanol product. The gaseous product enters the third flash kettle 5L for flash distillation again. The liquid product obtained by the third flash distillation is methanol product. The gaseous product is refluxed to the ninth pipeline 501 for recycling.

[0041] An Aspen Plus full-process simulation model of a process system for producing methanol from carbon dioxide hydrogenation coupled with chemical chain combustion was built, and the logistics results obtained are as follows: 50t / d of biomass is imported, and 1.1838kg / s of O2 is produced during the process of hydrogen production by electrolysis of water. 1.06542kg / s of pure O2 is input into the chemical chain combustion device to assist the chemical chain combustion of biomass, and the combustion efficiency of chemical chain combustion reaches more than 95%. Then 0.11838kg / s of pure O2 is introduced into the pure oxygen afterburner, and the combustion efficiency reaches more than 99%. The outlet gas of the pure oxygen afterburner is condensed to obtain 1.08947kg / s of CO2 with a purity of 99.63% (impurities are a small amount of N2 and H2O) and 0.386126kg / s H2O. This part of condensed water and 0.946831 kg / s of make-up water are introduced into the electrolytic cell for electrolysis reaction, and 1.1838 kg / s of high-purity O2 and 0.149155 kg / s of high-purity H2 are obtained. This part of H2 and CO2 are introduced into the carbon dioxide hydrogenation to methanol reactor to prepare methanol. The reaction stage temperature is 250 ° C, and finally 0.7715 kg / s of methanol with a purity of 99.19% is obtained. The logistics and energy flows can be balanced. Under these conditions, the biomass carbon conversion rate reaches 99.99%, the carbon capture efficiency reaches 99%, the CO2 conversion rate reaches 98%, and the methanol selectivity is 99%.

[0042] It will be easily understood by those skilled in the art that the above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A device for producing methanol by hydrogenation of carbon dioxide combined with chemical looping combustion, characterized in that: The invention comprises a power generation system (1), an electrolytic cell (2), a chemical chain combustion reactor (3), a pure oxygen afterburning chamber (4), and a methanol reaction unit (5). The power generation system (1) is connected to the electrolytic cell (2), the electrolytic cell (2) is connected to the chemical chain combustion reactor (3) through a first pipeline (101), the electrolytic cell (2) is connected to the pure oxygen afterburning chamber (4) through a second pipeline (111), the chemical chain combustion reactor (3) is connected to a raw material pipeline (104), the top of the chemical chain combustion reactor (3) is connected to the pure oxygen afterburning chamber (4) through a third pipeline (105), the pure oxygen afterburning chamber (4) is connected to the methanol reaction unit (5) through a fourth pipeline (109), the hydrogen generated by electrolysis of the electrolytic cell (2) is connected to the methanol reaction unit (5) through a fifth pipeline (102), and the methanol reaction unit (5) is connected to a sixth pipeline (110).

2. The device for producing methanol from carbon dioxide by hydrogenation combined with chemical looping combustion according to claim 1, characterized in that: The chemical chain combustion reactor (3) comprises a fuel reactor (31), a first cyclone separator (32), a second cyclone separator (35), an air reactor (33), a first flow sealing valve (34), and a second flow sealing valve (36); the fuel reactor (31) is connected to the first pipeline (101), the top of the fuel reactor (31) is connected to the top of the air reactor (33) through the first cyclone separator (32), and the top of the fuel reactor (31) is also connected to the pure oxygen supplementary valve (34) through the second cyclone separator (35). The top of the combustion chamber (4) is connected; the bottom of the fuel reactor (31) is connected to the bottom of the air reactor (33) through the first flow sealing valve (34), and the bottom of the fuel reactor (31) is also connected to the bottom of the second cyclone separator (35) through the second flow sealing valve (36); the top of the air reactor (33) is connected to the seventh pipeline (107), the bottom of the air reactor (33) is connected to the air pipeline (106), and the top of the second cyclone separator (35) is connected to the third pipeline (105).

3. The device for producing methanol from carbon dioxide by hydrogenation combined with chemical looping combustion according to claim 1, characterized in that: The fourth pipeline (109) is connected to a condenser (6), and the condenser (6) is connected to the electrolytic cell (2) via an eighth pipeline (108).

4. The device for producing methanol by hydrogenation of carbon dioxide combined with chemical looping combustion according to claim 1, characterized in that: The methanol reaction unit (5) specifically comprises: a first heat exchanger (5A), a fixed bed reactor (5B), a first flash kettle (5C), a second flash kettle (5D), a fractionator (5E), and a third flash kettle (5F) which are connected in sequence; the second pipeline (102) is connected to the fourth pipeline (109) and the ninth pipeline (501); the ninth pipeline (501) is connected to the first heat exchanger (5A); the tops of the first flash kettle (5C), the second flash kettle (5D), and the third flash kettle (5F) are connected to the ninth pipeline (501) via the tenth pipeline (502), the eleventh pipeline (503), and the twelfth pipeline (504), respectively; and the first heat exchanger (5A) is connected to the seventh pipeline (107).

5. The device for producing methanol by hydrogenation of carbon dioxide combined with chemical looping combustion according to claim 1, characterized in that: The raw material pipeline (104) is used to introduce biomass, and the fuel reactor (31) is loaded with an oxygen carrier, and the oxygen carrier is selected from one or more of Fe2O3, CuO, NiO, Mn2O3, CaSO4, BaSO4, CaFe2O5, CuFe2O4, and perovskite; the biomass is selected from one or more of sawdust, straw, and rice husk.

6. The device for producing methanol by hydrogenation of carbon dioxide combined with chemical looping combustion according to claim 1, characterized in that: The pure oxygen afterburning chamber (4) is filled with a mixture of a single substance or compound containing a precious metal or a non-precious metal element and Fe2O3, CuO, NiO, Mn2O3, Co3O4, or perovskite as a catalyst, wherein the precious metal is selected from Ag, Pd, Pt, Au, Rh, and Ir; and the non-precious metal is selected from Mn, Ce, and Sr; The fixed bed reactor (5B) is filled with a methanol synthesis catalyst, and the methanol synthesis catalyst is selected from one or more of Cu and Pd.

7. The method for preparing methanol from a device for preparing methanol from carbon dioxide hydrogenation combined with chemical looping combustion according to any one of claims 1 to 6, characterized in that: The steps include: (1) supplying power to an electrolytic cell through a power generation system, and the electrolytic cell electrolyzes water to produce hydrogen and oxygen; (2) introducing biomass, oxygen carrier, and oxygen produced by electrolyzed water with a volume fraction of 80 to 90% into the bottom of a chemical looping combustion reactor; (3) introducing the gas generated after the reaction in step (2) together with oxygen generated by electrolysis of water with a volume fraction of 10 to 20% into a pure oxygen afterburner, and further reacting under the action of a catalyst to completely convert the biomass into carbon dioxide gas; (4) The carbon dioxide and hydrogen obtained by electrolysis of water are combined to form a raw gas, and the raw gas is introduced into a methanol reaction unit to obtain methanol.

8. The method for preparing methanol from a device for preparing methanol from carbon dioxide hydrogenation combined with chemical looping combustion according to claim 7, characterized in that: Step (2) is specifically as follows: biomass is introduced into a fuel reactor containing an oxygen carrier for reaction; the gas generated by the reaction is separated into gas and solid by a second cyclone separator; the separated gas phase is introduced into a pure oxygen afterburning chamber for further reaction; the separated solid phase is returned to the fuel reactor through a second flow sealing valve; the oxygen carrier at the bottom of the fuel reactor enters the bottom of the air reactor through a first flow sealing valve; after fully reacting with the air introduced into the air reactor, it enters the first cyclone separator for gas and solid separation; the separated solid is the oxidized oxygen carrier, which falls into the fuel reactor to achieve circulation.

9. The method for preparing methanol from a device for preparing methanol from carbon dioxide hydrogenation combined with chemical looping combustion according to claim 8, characterized in that: Step (4) specifically comprises the following steps: the feed gas is introduced into a first heat exchanger, the tail gas of the air reactor produced in the air reactor is heat exchanged with the feed gas in the first heat exchanger to heat the feed gas, and the feed gas temperature is maintained at 200-300° C. The heated feed gas is sequentially introduced into a fixed bed reactor, a first flash kettle, a second flash kettle, a fractionator, and a third flash kettle for sufficient reaction, the third flash kettle flashes to produce a liquid product, methanol, and the gaseous product produced by the reaction of the first flash kettle, the second flash kettle, and the third flash kettle is returned to the feed gas for further sufficient reaction.

10. The method for preparing methanol from a device for preparing methanol from carbon dioxide hydrogenation combined with chemical looping combustion according to claim 9, characterized in that: The carbon dioxide gas produced in step (3) is condensed by a condenser, and the produced condensed water is passed into the electrolytic cell.

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