Biomass gasification coupled with soec electrolysis to produce methanol synthesis process

Abstract

The application relates to the field of renewable energy efficient storage technology, in particular to a biomass gasification coupling SOEC electrolysis methanol synthesis process. The process comprises the following steps: waste biomass fuel is gasified through a gasification furnace, and then is purified through first-stage purification, second-stage purification, third-stage purification and fourth-stage purification to obtain high-carbon synthesis gas; water vapor and the high-carbon synthesis gas are introduced into an SOEC electrolysis system to generate co-electrolysis, CO and H2 generated by the co-electrolysis are introduced into a methanol catalytic synthesis tower to react and synthesize methanol, the methanol is condensed to obtain liquid methanol, and unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through a pipeline to participate in the synthesis gas hydrogenation modulation in a cycle. The application provides the biomass gasification coupling SOEC electrolysis methanol synthesis process, CO2 in the whole methanol preparation process is recycled, green wind power and photovoltaic poor-quality electric energy are efficiently utilized, and energy efficiency and methanol yield are significantly improved.

Description

Technical Field

[0001] This application relates to the field of efficient renewable energy storage technology, specifically to a biomass gasification coupled SOEC electrolysis process for methanol synthesis. Background Technology

[0002] With the escalating energy crisis and environmental pollution, the development of clean alternative energy sources is attracting increasing attention. Biomass energy, with its abundant resources, renewability, and ability to achieve zero greenhouse gas emissions, has the potential to become the world's largest renewable and clean energy source. Thermochemical gasification catalytic synthesis of methanol from straw-based biomass is one of the most efficient biomass energy conversion technologies. The biomass gasification to methanol synthesis can be divided into two steps: the first step involves the thermochemical gasification of biomass to produce feed gas, which is then purified and treated with hydrogen to produce syngas; the second step involves the syngas undergoing catalytic synthesis of crude methanol under specific pressure and temperature conditions, followed by distillation to obtain the final methanol product.

[0003] Both domestic and international researchers have studied related technologies. The Hynol Process project in the United States achieves methanol production through three steps: 1. Biomass is converted into CO, H2, and CH4 in a hydrogasification furnace; 2. The mixed gas is reformed with steam and additional natural gas, and CH4 reacts with steam to produce CO and H2; 3. CO and H2 are synthesized into methanol at 3 MPa and 260℃. A domestic patent application by Chengdu Ruixun Technology Co., Ltd., entitled "A System and Method for Producing Fuel Oil from Biomass via Methanol," provides another route for producing methanol using biomass fuel: biomass pyrolysis or gasification is used to generate electricity, and the resulting green electricity is used to electrolyze water to produce green hydrogen and green oxygen. The green hydrogen is then combined with CO and CO2 obtained from biomass pyrolysis or gasification to synthesize green methanol. Additionally, a patent application by Sinochem Science and Technology Research Co., Ltd., entitled "A System and Method for Producing Methanol from Biomass Raw Materials," uses biomass syngas for dry reforming and adjusts the hydrogen-to-carbon ratio of the reformed gas by adding hydrogen before methanol synthesis.

[0004] The aforementioned traditional biomass-to-methanol technologies mainly fall into two technical pathways: First, biomass gasification yields CO, H2, and CH4, with the byproduct CH4 being reformed into CO and H2 via steam reforming, from which methanol is then synthesized. Second, biomass gasification yields CO, CO2, and H2, and hydrogenation is used to adjust the hydrogen-to-carbon ratio in the mixed gas, thereby increasing the methanol synthesis yield. While traditional biomass-to-methanol synthesis technologies achieve green methanol production throughout the entire process, they suffer from drawbacks such as low energy utilization (biomass power generation followed by water electrolysis, and CH4 reformed into CO and H2 via steam reforming), low CO2 recycling rate, and low waste heat recycling rate. Summary of the Invention

[0005] To address the aforementioned issues, the purpose of this application is to provide a biomass gasification coupled SOEC electrolysis process for methanol synthesis, in which CO2 is recycled throughout the entire methanol production process, while simultaneously making efficient use of green wind power and low-quality photovoltaic power, resulting in a significant improvement in energy efficiency and methanol yield.

[0006] To achieve the above objectives, this application provides a biomass gasification coupled with SOEC electrolysis to produce methanol, comprising the following steps: S1. Waste biomass fuel is gasified in a gasifier, and then purified through primary, secondary, tertiary and quaternary purification to obtain high-carbon syngas. In the above process, the gasifier is equipped with a tar catalytic cracking unit, which aims to reduce the tar content from the source, reduce the burden of subsequent purification, and increase the H2 / CO ratio. The four-stage purification process is progressively more thorough. The first stage of purification removes large particulate dust, the second stage removes most of the sulfur, halides and other harmful impurities, the third stage cracks the residual tar, recombines the syngas, and adjusts the H2 / CO ratio to obtain high-quality hydrogen-rich syngas, the fourth stage syngas is heat-exchanged by a high-temperature heat exchanger to adjust the temperature and control the gas water content, then enters a gas-liquid separator to separate liquid water, and finally enters a fine desulfurization tank to deeply remove inorganic sulfur and organic sulfur, ensuring that the total sulfur content of the outlet process gas is low, so as to effectively protect the downstream methanol synthesis catalyst. The chemical equation for inorganic sulfur desulfurization is: ZnO + H₂S = ZnS + H₂O + 76.62 kJ / mol The hydrolysis reaction equation for organic sulfur is: COS + H2O = H2S + CO2 + 35.53 kJ / mol.

[0007] S2. Water vapor and high-carbon syngas are fed into the SOEC electrolysis system for co-electrolysis. The generated CO and H2 are fed into the methanol catalytic synthesis tower to react and synthesize methanol. After condensation, liquid methanol is obtained. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

[0008] In the above process, the water vapor is the high-temperature water vapor generated during methanol synthesis. The channels for the high-carbon synthesis gas to enter the SOEC electrolysis system are equipped with mass flow meters for flow monitoring. CO2 and water vapor undergo co-electrolysis, producing CO and H2 at the cathode and high-purity oxygen at the anode. The higher the water vapor content, the higher the hydrogen content of the cathode tail gas. The tail gas outlet gas from the SOEC electrolysis system is cooled by heat exchange in the gasifier and then fed into the methanol catalytic synthesis tower to react and synthesize methanol. The methanol synthesis equation is: CO + 2H2 → CH3OH.

[0009] Furthermore, the waste biomass fuel is at least one of crop straw, forest residue, timber mill waste, organic components of municipal solid waste, and livestock and poultry manure.

[0010] Furthermore, the gasifier is equipped with a tar catalytic cracking device, and the catalyst is a Ni-based catalyst or dolomite.

[0011] Preferably, the gasifier is equipped with a tar catalytic cracking device, and the catalyst is a Ni-based catalyst.

[0012] Furthermore, the gasification in the gasifier is carried out under the following conditions: a gasification temperature of 800-1000℃ and an air-to-water vapor volume ratio of 0.25-0.35.

[0013] Furthermore, the primary purification stage employs a cyclone separator to remove particulate matter, with the following operating parameters: inlet flow velocity of 15-25 m / s, operating temperature of 300-500℃, and pressure drop of 1-2 kPa.

[0014] Furthermore, the secondary purification process employs activated carbon adsorption to remove sulfides and halides at an adsorption temperature of 20-50°C and a space velocity of 200-400 h⁻¹. -1 .

[0015] Furthermore, the three-stage purification process employs plasma recombination into gas, with a reaction temperature of 1000-1200℃. The plasma source is a non-transfer arc plasma torch, and the working gas is nitrogen or argon.

[0016] Furthermore, the fourth-stage purification is a fine desulfurization step, employing a multi-layer composite bed design. The upper layer is an activated alumina protective layer, with a filling height accounting for 10-15% of the total filling height of the desulfurization tank. The operating temperature is 25-40℃, and the space velocity is 1000-3000 h⁻¹. -1 The middle layer is a zinc oxide desulfurizing agent to remove inorganic sulfur, and its filling height accounts for 60-70% of the total filling height of the desulfurization tank. The operating temperature is 30-50℃, and the space velocity is 1000-2000 h⁻¹. -1 The lower layer uses a cobalt-molybdenum or nickel-molybdenum hydroconversion catalyst to remove organic sulfur, with an operating temperature of 200-300℃ and a space velocity of 500-1500 h⁻¹. -1 .

[0017] Furthermore, the CO and H2 are introduced into the methanol catalytic synthesis tower, and the molar ratio of CO to H2 is 1:2.2-3.0.

[0018] Furthermore, the methanol synthesis is carried out at a temperature of 230-270℃ and a pressure of 5-10MPa, using CuO / ZnO / Al2O3 or CuO / ZnO / Cr2O3 as the catalyst.

[0019] In summary, this application has the following beneficial effects: The overall scheme of biomass fuel pyrolysis gasification - renewable energy-driven SOEC CO2 reduction and hydrogen supplementation - copper-based catalytic synthesis - methanol condensation and collection, hydrocarbon recycling and modulation utilization is proposed. This scheme is designed for the western region with abundant renewable energy and biomass fuel. It proposes a technological path for the industrialization and large-scale conversion of renewable energy with SOEC as the core. It can convert waste electricity and biomass energy into green methanol, an industrial energy source, on a large scale. It provides a specific technical path for the efficient preparation and storage of renewable energy, making it possible for the large-scale and efficient transportation and use of renewable energy.

[0020] Renewable energy drives SOEC electrolysis systems to supplement hydrogen sources for biomass fuel syngas. Based on the traditional CO and H2 to methanol synthesis process, and taking advantage of the resource advantages of western China, SOEC green hydrogen sources are used as a supplement. By making full use of the high carbon and high hydrogen syngas from biomass and adjusting the hydrogen-carbon ratio, green methanol is efficiently produced while achieving efficient recycling of wind and solar power and CO2.

[0021] High-grade heat energy from SOEC emissions is directly injected into the gasifier as the driving force for the reaction, eliminating the waste of high-quality energy. Medium-grade reaction heat released from methanol synthesis is used to generate steam to drive the core equipment. Low-grade waste heat is collected and recovered for deep drying of biomass feedstock. This application accurately identifies the heat grades of exhaust gases from the three stages of biomass gasification, SOEC electrolysis, and methanol synthesis, utilizing them in stages to achieve efficient heat energy recycling and improve overall efficiency. Attached Figure Description

[0022] To more clearly illustrate the technical solutions of the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 This is a process flow diagram for this application. Detailed Implementation

[0024] The technical solutions in the embodiments of this application will be clearly and completely described below with reference to the embodiments of this application. Obviously, the described embodiments are only some embodiments of this invention, and not all embodiments. Based on the embodiments of this invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of this invention.

[0025] The raw materials used in the specific embodiments of this application are analytical grade. Additionally: the activated alumina is spherical with a particle size of 4 mm; the zinc oxide desulfurizer is spherical with a particle size of 3 mm; and the Co-Mo / Al2O3 is strip-shaped with a particle size of 2 mm.

[0026] Example 1 A biomass gasification coupled with SOEC electrolysis to produce methanol synthesis process includes the following steps: S1. A downdraft fixed-bed gasifier is used to process wheat straw, equipped with a tar catalytic cracking unit (Ni-based catalyst). The gasification temperature is controlled at 800℃ and the air-to-water vapor volume ratio is 0.25 to obtain syngas. Then, it undergoes primary purification (using a cyclone separator to remove particulate matter, inlet flow rate of 15m / s, operating temperature of 300℃, and pressure drop of 1kPa) and secondary purification (using activated carbon adsorption to remove sulfides and halides, adsorption temperature of 20℃, and space velocity of 200h⁻¹). -1 Three-stage purification (using plasma recombination to form gas, reaction temperature 1000℃, plasma source is non-transfer arc plasma torch, working gas is nitrogen), and four-stage purification (fine desulfurization, using multi-layer composite bed design, upper layer is active alumina protective layer, filling height accounts for 10% of the total filling height of the desulfurization tank, operating temperature 25℃, space velocity is 1000h). -1 The middle layer contains zinc oxide desulfurizer to remove inorganic sulfur, and its filling height accounts for 60% of the total filling height of the desulfurization tank. The operating temperature is 30℃, and the space velocity is 1000 h⁻¹. -1 The lower layer contains a Co-Mo / Al2O3 hydroconversion catalyst for removing organic sulfur, with a packing height accounting for 30% of the total packing height of the desulfurization tank. The operating temperature is 200℃ and the space velocity is 500 h⁻¹. -1 ), to obtain high-carbon syngas; S2. Water vapor and high-carbon syngas are introduced into the SOEC electrolysis system. CO2 and water vapor in the high-carbon syngas undergo co-electrolysis, producing CO and H2 at the anode and high-purity oxygen at the cathode. CO and H2 are fed into the methanol catalytic synthesis tower at a molar ratio of 1:2.2 to synthesize methanol (temperature 230℃, pressure 5MPa, catalyst is CuO / ZnO / Al2O3). The mixture is condensed at 30℃ to obtain liquid methanol. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

[0027] Example 2 A biomass gasification coupled with SOEC electrolysis to produce methanol synthesis process includes the following steps: S1. A downdraft fixed-bed gasifier is used to process wheat straw, equipped with a tar catalytic cracking unit (Ni-based catalyst). The gasification temperature is controlled at 900℃ and the air-to-water vapor volume ratio is 0.3 to obtain syngas. Then, it undergoes primary purification (using a cyclone separator to remove particulate matter, inlet flow rate of 20m / s, operating temperature of 400℃, and pressure drop of 1kPa) and secondary purification (using activated carbon adsorption to remove sulfides and halides, adsorption temperature of 35℃, and space velocity of 300h⁻¹). -1 Three-stage purification (using plasma recombination to form gas, reaction temperature 1100℃, plasma source is a non-transfer arc plasma torch, working gas is nitrogen), four-stage purification (fine desulfurization, using a multi-layer composite bed design, the upper layer is an activated alumina protective layer, the filling height accounts for 15% of the total filling height of the desulfurization tank, operating temperature 30℃, space velocity is 2000h). -1 The middle layer contains zinc oxide desulfurizer to remove inorganic sulfur, and its filling height accounts for 65% of the total filling height of the desulfurization tank. The operating temperature is 40℃, and the space velocity is 1500 h⁻¹. -1 The lower layer contains a Co-Mo / Al2O3 hydroconversion catalyst for removing organic sulfur, accounting for 20% of the total packing height of the desulfurization tank. The operating temperature is 250℃ and the space velocity is 1000 h⁻¹. -1 ), to obtain high-carbon syngas; S2. Water vapor and high-carbon syngas are introduced into the SOEC electrolysis system. CO2 and water vapor in the high-carbon syngas undergo co-electrolysis, producing CO and H2 at the anode and high-purity oxygen at the cathode. CO and H2 are fed into the methanol catalytic synthesis tower at a molar ratio of 1:2.6 to synthesize methanol (temperature 250℃, pressure 8MPa, catalyst is CuO / ZnO / Al2O3). The mixture is condensed at 30℃ to obtain liquid methanol. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

[0028] Example 3 A biomass gasification coupled with SOEC electrolysis to produce methanol synthesis process includes the following steps: S1. A downdraft fixed-bed gasifier is used to process wheat straw, equipped with a tar catalytic cracking unit (Ni-based catalyst). The gasification temperature is controlled at 1000℃ and the air-to-water vapor volume ratio is 0.35 to obtain syngas. Then, it undergoes primary purification (using a cyclone separator to remove particulate matter, inlet flow rate of 25m / s, operating temperature of 500℃, and pressure drop of 1kPa) and secondary purification (using activated carbon adsorption to remove sulfides and halides, adsorption temperature of 50℃, and space velocity of 400h⁻¹). -1Three-stage purification (using plasma recombination to form gas, reaction temperature 1200℃, plasma source is non-transfer arc plasma torch, working gas is nitrogen), four-stage purification (fine desulfurization, using multi-layer composite bed design, upper layer is active alumina protective layer, filling height accounts for 15% of the total filling height of the desulfurization tank, operating temperature 40℃, space velocity is 3000h). -1 The middle layer is a zinc oxide desulfurizing agent used to remove inorganic sulfur, and its filling height accounts for 70% of the total filling height of the desulfurization tank. The operating temperature is 50℃, and the space velocity is 2000 h⁻¹. -1 The lower layer contains a Co-Mo / Al2O3 hydroconversion catalyst for removing organic sulfur, accounting for 15% of the total packing height of the desulfurization tank. The operating temperature is 300℃ and the space velocity is 1500 h⁻¹. -1 ), to obtain high-carbon syngas; S2. Water vapor and high-carbon syngas are introduced into the SOEC electrolysis system. CO2 and water vapor in the high-carbon syngas undergo co-electrolysis, producing CO and H2 at the anode and high-purity oxygen at the cathode. CO and H2 are fed into the methanol catalytic synthesis tower at a molar ratio of 1:3.0 to synthesize methanol (temperature 270℃, pressure 10MPa, catalyst is CuO / ZnO / Al2O3). The mixture is condensed at 30℃ to obtain liquid methanol. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

[0029] Compare with Example 1 The difference between this comparative example and Example 3 is that a low-temperature proton exchange membrane electrolysis system is used instead of an SOEC electrolysis system.

[0030] Compare with Example 2 The difference between this comparative example and Example 3 is that the present application discloses a biomass gasification coupled with SOEC electrolysis to produce methanol, which includes the following steps: S1. Wheat straw is treated using a hydrogenation gasification furnace, with the gasification temperature controlled at 1000℃ and the air-to-water vapor volume ratio at 0.35 to obtain syngas. This syngas then undergoes primary purification (using a cyclone separator to remove particulate matter, with an inlet velocity of 25 m / s, operating temperature of 500℃, and pressure drop of 1 kPa) and secondary purification (using activated carbon adsorption to remove sulfides and halides, with an adsorption temperature of 50℃ and a space velocity of 400 h⁻¹). -1 Three-stage purification (using plasma recombination to form gas, reaction temperature 1200℃, plasma source is non-transfer arc plasma torch, working gas is nitrogen), four-stage purification (fine desulfurization, using multi-layer composite bed design, upper layer is active alumina protective layer, filling height accounts for 15% of the total filling height of the desulfurization tank, operating temperature 40℃, space velocity is 3000h). -1The middle layer is a zinc oxide desulfurizing agent used to remove inorganic sulfur, and its filling height accounts for 70% of the total filling height of the desulfurization tank. The operating temperature is 50℃, and the space velocity is 2000 h⁻¹. -1 The lower layer contains a Co-Mo / Al2O3 hydroconversion catalyst for removing organic sulfur, accounting for 15% of the total packing height of the desulfurization tank. The operating temperature is 300℃ and the space velocity is 1500 h⁻¹. -1 ), to obtain high-carbon syngas; S2. Water vapor and high-carbon syngas are introduced into the SOEC electrolysis system. CO2 and water vapor in the high-carbon syngas undergo co-electrolysis, producing CO and H2 at the anode and high-purity oxygen at the cathode. CO and H2 are fed into the methanol catalytic synthesis tower at a molar ratio of 1:3.0 to synthesize methanol (temperature 270℃, pressure 10MPa, catalyst is CuO / ZnO / Al2O3). The mixture is condensed at 30℃ to obtain liquid methanol. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

[0031] Performance testing Functional tests were conducted on the methanol preparation processes of Examples 1-3 and Comparative Examples 1-2.

[0032] The methanol production yield from processing 1 ton of wheat straw was compared using the methanol preparation processes of Examples 1-3 and Control Examples 1-2. The test results are shown in Table 1. Table 1

[0033] As shown in Table 1, the methanol production processes in Examples 1-3 of this application produce a high methanol yield, while the methanol yields in Comparative Examples 1 and 2 are relatively low, not as high as those in the examples of this application. This application, through deep purification, deep tar cracking, and SOEC circulating electrolysis, converts CO2 and circulating gas back into raw materials, locking carbon elements within the process for repeated utilization, thereby increasing methanol production. Furthermore, this application has a simple process, zero carbon emissions, and utilizes renewable energy sources such as photovoltaic and wind power, as well as the heat energy generated during the process, achieving efficient energy utilization. Comparative Example 1 uses a low-temperature proton exchange membrane. The water electrolysis system replaces the SOEC electrolysis system. Although the low-temperature proton exchange membrane water electrolysis system is a high-quality electric energy driven water electrolysis system, it does not have the ability to utilize renewable energy sources such as wind and solar power curtailment, capture CO2 greenhouse gas, or efficiently utilize waste heat from the cycle. The gasifier used in Comparative Example 2 is a hydrogenation gasifier, but the concentration of CH4, a byproduct of the reaction, is high, requiring the addition of a subsequent reforming unit to convert CH4 into CO and hydrogen, which significantly increases the complexity of the system and reduces energy efficiency. The effects achieved by Comparative Examples 1 and 2 are not as good as those of Example 3 of this application.

[0034] The above description is merely an example and illustration of the concept of this application. Those skilled in the art can make various modifications or additions to the specific embodiments described or use similar methods to replace them, as long as they do not deviate from the inventive concept or exceed the scope defined in the claims, they should all fall within the protection scope of this application.

Claims

1. A process for synthesizing methanol from biomass gasification coupled with SOEC electrolysis, characterized in that, Includes the following steps: S1. Waste biomass fuel is gasified in a gasifier, and then purified through primary, secondary, tertiary and quaternary purification to obtain high-carbon syngas. S2. Water vapor and high-carbon syngas are fed into the SOEC electrolysis system for co-electrolysis. The generated CO and H2 are fed into the methanol catalytic synthesis tower to react and synthesize methanol. After condensation, liquid methanol is obtained. Unreacted H2, CO and water are returned to the front end of the SOEC electrolysis system through pipelines and recycled to participate in the hydrogenation modulation of syngas.

2. The biomass gasification coupled SOEC electrolysis process for methanol synthesis according to claim 1, characterized in that, The gasifier is equipped with a tar catalytic cracking device, and the catalyst is a Ni-based catalyst or dolomite.

3. The biomass gasification coupled SOEC electrolysis process for methanol synthesis according to claim 2, characterized in that, The gasifier is equipped with a tar catalytic cracking device, and the catalyst is a Ni-based catalyst.

4. The biomass gasification coupled SOEC electrolysis process for methanol synthesis according to claim 1, characterized in that, The gasifier is used for gasification under the following conditions: gasification temperature 800-1000℃, and air to water vapor volume ratio 0.25-0.

35.

5. The process for synthesizing methanol from biomass gasification coupled with SOEC electrolysis according to claim 1, characterized in that, The primary purification stage uses a cyclone separator to remove particulate matter. The operating parameters are: inlet flow velocity of 15-25 m / s, operating temperature of 300-500℃, and pressure drop of 1-2 kPa.

6. The process for synthesizing methanol from biomass gasification coupled with SOEC electrolysis according to claim 1, characterized in that, The secondary purification process employs activated carbon adsorption to remove sulfides and halides at an adsorption temperature of 20-50℃ and a space velocity of 200-400 h⁻¹. -1 .

7. The process for synthesizing methanol from biomass gasification coupled with SOEC electrolysis according to claim 1, characterized in that, The three-stage purification process employs plasma recombination into gas, with a reaction temperature of 1000-1200℃. The plasma source is a non-transfer arc plasma torch, and the working gas is nitrogen or argon.

8. The process for synthesizing methanol from biomass gasification coupled with SOEC electrolysis according to claim 1, characterized in that, The fourth-stage purification is a fine desulfurization step, employing a multi-layer composite bed design. The upper layer is an activated alumina protective layer, with a filling height accounting for 10-15% of the total filling height of the desulfurization tank. The operating temperature is 25-40℃, and the space velocity is 1000-3000 h⁻¹. -1 The middle layer is a zinc oxide desulfurizing agent to remove inorganic sulfur, and its filling height accounts for 60-70% of the total filling height of the desulfurization tank. The operating temperature is 30-50℃, and the space velocity is 1000-2000 h⁻¹. -1 The lower layer uses a cobalt-molybdenum or nickel-molybdenum hydroconversion catalyst to remove organic sulfur, with an operating temperature of 200-300℃ and a space velocity of 500-1500 h⁻¹. -1 .

9. The biomass gasification coupled SOEC electrolysis process for methanol synthesis according to claim 1, characterized in that, The CO and H2 are introduced into the methanol catalytic synthesis tower, and the molar ratio of CO to H2 is 1:2.2-3.

0.

10. The biomass gasification coupled SOEC electrolysis process for methanol synthesis according to claim 1, characterized in that, The methanol synthesis is carried out at a temperature of 230-270℃ and a pressure of 5-10MPa, using CuO / ZnO / Al2O3 or CuO / ZnO / Cr2O3 as the catalyst.

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