A method for preparing a catalyst for syngas production and its application.

Abstract

This application relates to a method for preparing a catalyst for syngas production and its application. The method includes: dissolving a metal salt in water and stirring once to obtain a metal salt solution; adding alumina powder to the metal salt solution and stirring and allowing it to stand twice to obtain metal-loaded alumina; mixing and aging the metal-loaded alumina with a binder, extrusion aid, peptizing agent, and water sequentially to obtain a wet material; and extruding, drying, and calcining the wet material sequentially to obtain the catalyst. Through precise catalyst design, the co-conversion reaction of biomass and carbon dioxide can be efficiently catalyzed, achieving highly selective syngas production. This not only provides a core process pathway for the high-value utilization of biomass and the resource recovery of carbon dioxide but also simultaneously achieves the dual goals of carbon emission reduction and resource recycling. In the treatment of industrial carbon sources such as steel plant tail gas, the catalyst exhibits excellent activity, stability, and industrial application potential.

Description

Technical Field

[0001] This application relates to the field of biomass carbon dioxide resource utilization technology, and in particular to a method for preparing a catalyst for producing syngas and the application of the catalyst. Background Technology

[0002] Biomass gasification technology, by converting biomass resources into syngas (mainly composed of CO and H2), provides an important pathway for the supply of clean energy and chemical raw materials. This syngas can serve as a basic raw material for chemical synthesis and as a reducing agent in metallurgical processes; therefore, achieving efficient syngas production is of significant strategic importance for building a green circular economy system. In this process, introducing carbon dioxide as a gasifying agent in biomass conversion not only transforms carbon dioxide into useful resources but also simultaneously enhances the conversion value of biomass waste, thereby achieving synergistic effects of carbon cycling and waste value-added processing.

[0003] However, current biomass-carbon dioxide co-conversion systems generally suffer from low reaction rates, low carbon conversion efficiency, and insufficient syngas yield due to the inherently endothermic reaction and significant thermodynamic equilibrium limitations. Meanwhile, traditional catalysts are prone to carbon deposition, deactivation, and sintering under reaction conditions, and their mechanical strength and long-term stability are insufficient for continuous industrial operation. In summary, existing catalysts often struggle to simultaneously achieve high activity, high mechanical strength, resistance to carbon deposition, and good stability, resulting in significant obstacles to the large-scale practical application of this technology. Summary of the Invention

[0004] This application provides a method for preparing a catalyst for producing syngas and the application of the catalyst, in order to solve the following technical problems: how to solve the problems of low catalyst activity, poor mechanical strength, easy carbon deposition and sintering.

[0005] In a first aspect, embodiments of this application provide a method for preparing a catalyst for producing syngas, the method comprising:

[0006] The metal salt is dissolved in water and stirred once to obtain a metal salt solution; Alumina powder was added to the metal salt solution and stirred and allowed to stand twice to obtain metal-loaded alumina. The alumina loaded with the metal is mixed with binder, extrusion aid, adhesive solvent and water in sequence and then aged to obtain a wet material; The wet material is sequentially extruded, dried, and calcined to obtain the catalyst.

[0007] Optionally, the metal salt is at least one of rare earth metal salts, transition metal salts, and alkali metal salts.

[0008] Optionally, the total metal content of the metal salt solution is ≤30wt%.

[0009] Optionally, the content of the alumina powder is 65wt% to 85wt%.

[0010] Optionally, the alumina powder is spherical, and the average particle size of the alumina powder is 300nm~500nm.

[0011] Optionally, the stirring time for one stirring session is 10 min to 30 min.

[0012] Optionally, the secondary stirring time is 0.5h to 4.0h.

[0013] Optionally, the settling time is ≤48h.

[0014] Optionally, the content of the adhesive is 15wt% to 35wt%.

[0015] Optionally, the binder is at least one selected from silica sol, alumina sol, SB powder, kaolin, clay, and diatomaceous earth.

[0016] Optionally, the mass of the extrusion aid is 2% to 7% of the total mass of the alumina powder and the binder.

[0017] Optionally, the extrusion aid is at least one of guar gum powder and glycerin.

[0018] Optionally, the total mass of the adhesive solvent and the water is 30% to 80% of the total mass of the alumina powder and the binder.

[0019] Optionally, the adhesive solvent is at least one selected from nitric acid, hydrochloric acid, acetic acid, citric acid, and oxalic acid.

[0020] Optionally, the aging time is 6h to 12h.

[0021] Optionally, the drying temperature is 80℃~110℃, and the drying time is 8h~24h.

[0022] Optionally, the calcination temperature is 500℃~650℃, and the calcination time is 4h~8h.

[0023] Secondly, embodiments of this application provide an application of the catalyst prepared by the method described in the first aspect in the production of syngas. The catalyst is applied to the conversion of biomass carbon dioxide into syngas, and the catalyst catalyzes the conversion reaction of the syngas production. The reaction temperature of the conversion reaction is 700℃~1000℃.

[0024] The technical solutions provided in this application have the following advantages compared with the prior art: This application provides a method for preparing a catalyst for syngas production and its application. The method includes: dissolving a metal salt in water and stirring once to obtain a metal salt solution; adding alumina powder to the metal salt solution and stirring and allowing it to stand twice to obtain metal-loaded alumina; mixing and aging the metal-loaded alumina with a binder, extrusion aid, peptizing agent, and water sequentially to obtain a wet material; and extruding, drying, and calcining the wet material sequentially to obtain the catalyst. The method overcomes the problems of low catalyst activity, poor mechanical strength, easy carbon deposition, and sintering through multi-level structural synergistic design. In the active center construction stage, the multi-metal synergistic effect optimizes the electronic environment of the alumina surface, forming a strong bonded interface to anchor highly active metal particles, and eliminating activity decay caused by sintering by inhibiting high-temperature migration. In the forming process, precise control of aging parameters enables the binder and carrier to construct an interpenetrating network structure, which, after calcination, forms a multi-level porous system with interconnected channels and a high-strength framework. This structure protects the integrity of the catalyst surface while providing efficient channels for reactant diffusion and resisting structural stress caused by carbon deposition. Synchronous modulation of the surface electronic structure enhances the activation ability of carbon-oxygen bonds, promoting the conversion of deposited carbon into gaseous products and achieving in-situ removal.

[0025] In summary, based on the synergistic effect of active site stabilization, pore structure enhancement, and surface dynamic regeneration, this catalyst maintains high dispersion of active centers through strong metal-support interactions to block sintering deactivation, utilizes a multi-level pore system to inhibit carbon nucleus enrichment and enhance mechanical stability, and leverages surface electronic properties to drive in-situ gasification and removal of carbon deposits. Ultimately, it achieves high syngas selectivity, low deactivation rate, and long-term stable operation simultaneously during biomass carbon dioxide conversion, completely overcoming the deactivation problem caused by carbon deposits and sintering. Attached Figure Description

[0026] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with this application and, together with the description, serve to explain the principles of this application.

[0027] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the accompanying drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, those skilled in the art can obtain other drawings based on these drawings without any creative effort.

[0028] Figure 1 A flowchart illustrating a method for preparing a catalyst for producing syngas, provided as an embodiment of this application; Figure 2 A process flow diagram for biomass carbon dioxide conversion to syngas is provided for embodiments of this application; Figure 2In the middle section: 1-3, flow meter; 4, preheater; 5, screw feeder; 6, biomass; 7, gasifier; 8, heating furnace; 9, catalyst; 10, drying tube; 11, condenser; 12, gas-liquid separator; 13, gas analyzer. Detailed Implementation

[0029] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this application. All other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are within the scope of protection of this application.

[0030] The range descriptions used herein, such as numerical ranges and proportional ranges, include all possible sub-ranges and single numerical values ​​within that range. For example, the range descriptions of "1 to 6" or "1~6" cover all sub-ranges between 1 and 6 (such as 1 to 3, 2 to 5, etc.) and single numbers (such as 1, 2, 3, 4, 5, 6). Unless otherwise specified, the terms "including" and "contains" used herein mean "including but not limited to"; relational terms such as "first" and "second" are used only to distinguish different entities or operations and do not imply an actual order or relationship. "And / or" indicates that multiple situations can exist individually or simultaneously. Expressions such as "at least one," "multiple," and "at least one" refer to any combination of the corresponding objects, including combinations of single or multiple objects. The proportional relationships mentioned herein, such as mass ratios and molar ratios, should be understood as the correspondence between the first and second terms of a proportional formula, according to the order of description. The raw materials, reagents, instruments, and equipment used herein can all be obtained through commercial purchase or prepared using existing methods.

[0031] Figure 1 This is a flowchart illustrating a method for preparing a catalyst for producing syngas, as provided in an embodiment of this application.

[0032] Please see Figure 1 This application provides a method for preparing a catalyst for producing syngas, the method comprising: S1. Dissolve the metal salt in water and stir once to obtain a metal salt solution; S2. Add alumina powder to the metal salt solution and stir and let stand twice to obtain metal-loaded alumina. S3. The alumina loaded with the metal is mixed with binder, extrusion aid, adhesive solvent and water in sequence and aged to obtain wet material; S4. The wet material is sequentially extruded, dried, and calcined to obtain the catalyst.

[0033] In the above technical solution, the metal salt is first dissolved in water, and the active components are dispersed at the molecular level by stirring, providing a homogeneous precursor for subsequent loading. Then, the alumina powder is stirred and allowed to stand in the metal salt solution to complete the interfacial anchoring of the metal active centers. The metal loading methods include single-metal stepwise loading, multi-metal sequential loading, or multi-metal co-loading, forming a strong metal-support interaction that resists migration. Next, the loaded wet alumina is mixed directly or after drying into powder with binder, extrusion aid, adhesive solvent, and water. By controlling the rheological properties of the wet material and the self-assembly during the aging process, through-pores and a high-strength skeleton are formed. Finally, extrusion molding combined with gradient temperature field treatment achieves the directional arrangement of the active phase lattice while maintaining the multi-level porous structure, thereby simultaneously endowing the catalyst with high mechanical strength, anti-sintering properties, and dynamic anti-carbon deposition ability.

[0034] In some embodiments, the metal salt is at least one of rare earth metal salts, transition metal salts, and alkali metal salts.

[0035] The metal salt is at least one of rare earth metal salts, transition metal salts, and alkali metal salts. Among them, rare earth metal salts are used to regulate the electronic properties of the support surface, transition metal salts are responsible for constructing the main active centers, and alkali metal salts can enhance the catalyst's resistance to carbon deposition.

[0036] In some embodiments, the total metal content of the metal salt solution is ≤30wt%.

[0037] A total metal content of ≤30wt% in the metal salt solution ensures high dispersion of the active components, thus fully exposing active sites, while avoiding blockage of the support pores and increased mass transfer resistance due to excessive metal content. This ultimately achieves a synergistic improvement in catalyst activity and stability. For example, the total metal content of the metal salt solution can be 20wt%, 22wt%, 24wt%, 26wt%, 28wt%, 30wt%, etc.

[0038] In some embodiments, the content of the alumina powder is 65wt% to 85wt%.

[0039] The alumina powder content is between 65 wt% and 85 wt% to ensure that the catalyst has sufficient structural support and pore capacity, thereby laying the structural foundation for the uniform dispersion of the active components and mass transfer during the reaction process. For example, the alumina powder content can be 65 wt%, 75 wt%, 85 wt%, etc.

[0040] In some embodiments, the alumina powder is spherical, and the average particle size of the alumina powder is 300 nm to 500 nm.

[0041] The spherical shape of the alumina powder helps improve the uniformity of the active component loading and the overall flowability of the catalyst. The average particle size of the alumina powder is between 300 nm and 500 nm, which ensures a large specific surface area while enhancing its anti-agglomeration properties. This ensures that the active sites formed by the active components loaded on the alumina powder are fully exposed and inhibits sintering of the active components during high-temperature reactions. For example, the average particle size of the alumina powder can be 300 nm, 350 nm, 400 nm, 450 nm, or 500 nm.

[0042] In some embodiments, the stirring time is 10 min to 30 min.

[0043] A stirring time of 10 to 30 minutes ensures that the metal salt is fully dissolved, guaranteeing precise control of the stoichiometry of the precursor solution. Sufficient stirring also achieves uniform dispersion of metal ions, laying the foundation for obtaining a catalyst with highly dispersed metal species. For example, a stirring time of 10, 20, or 30 minutes can be used.

[0044] In some embodiments, the secondary stirring time is 0.5h to 4.0h.

[0045] The secondary stirring time is between 0.5h and 4.0h, which provides sufficient guarantee for the diffusion of metal ions into the alumina channels and the achievement of adsorption equilibrium on their inner and outer surfaces. This achieves uniform distribution across the entire range from the particle scale to the channel scale, avoiding local enrichment or surface accumulation of active components. For example, the secondary stirring time can be 0.5h, 1.5h, 2.5h, 3.5h, etc.

[0046] In some implementations, the settling time is ≤48h.

[0047] The settling time is ≤48h, which aims to promote the full adsorption and directional anchoring of the active metal components on the alumina carrier surface, while avoiding excessive hydration of the metal components due to prolonged settling, which could lead to the embedding of active sites and reduced accessibility. For example, the settling time can be 40h, 42h, 44h, 46h, 48h, etc.

[0048] In some embodiments, the content of the adhesive is 15wt% to 35wt%.

[0049] The binder content is between 15wt% and 35wt%, which can provide suitable plasticity and bonding strength for the catalyst precursor, thereby effectively maintaining the continuity of the multi-level pore structure inside the catalyst while ensuring the integrity of the extrusion molding. For example, the binder content can be 15wt%, 20wt%, 25wt%, 30wt%, 35wt%, etc.

[0050] In some embodiments, the binder is at least one selected from silica sol, alumina sol, SB powder, kaolin, clay, and diatomaceous earth.

[0051] The binder is at least one of silica sol, alumina sol, SB powder, kaolin, clay, and diatomaceous earth. Such binders can construct a chemically compatible bonding network within the catalyst, thereby effectively maintaining the continuity of the hierarchical pore structure while improving the overall mechanical strength of the catalyst.

[0052] In some embodiments, the mass of the extrusion aid is 2% to 7% of the total mass of the alumina powder and the binder.

[0053] The addition of extrusion aids aims to improve the plastic flow characteristics of wet materials. The mass of the extrusion aid is 2% to 7% of the total mass of alumina powder and binder. This ensures the continuity and smoothness of extrusion molding while preventing excessive extrusion aid from covering the active surface and affecting catalyst performance. For example, the mass of the extrusion aid can be 2%, 3%, 4%, 5%, 6%, 7% of the total mass of alumina powder and binder.

[0054] In some embodiments, the extrusion aid is at least one of guar gum powder and glycerin.

[0055] The extrusion aid is at least one of guar gum powder and glycerol. Guar gum powder can improve the plasticity of wet materials, while glycerol can adjust the rheological properties of the system. Together, they ensure the continuity of the extrusion process and are beneficial to improving the surface smoothness of the catalyst.

[0056] In some embodiments, the total mass of the adhesive solvent and the water is 30% to 80% of the total mass of the alumina powder and the binder.

[0057] The total mass of the adhesive solvent and water is between 30% and 80% of the total mass of the alumina powder and binder. Within this range, the liquid medium can effectively activate the carrier surface and regulate the slurry viscosity through acid hydrolysis and wetting, thereby providing suitable kinetic conditions for the self-assembly of pores during subsequent aging. For example, the total mass of the adhesive solvent and water can be 30%, 40%, 50%, 60%, 70%, 80%, etc., of the total mass of the alumina powder and binder.

[0058] In some embodiments, the adhesive solvent is at least one selected from nitric acid, hydrochloric acid, acetic acid, citric acid, and oxalic acid.

[0059] The adhesive solvent is at least one of nitric acid, hydrochloric acid, acetic acid, citric acid, and oxalic acid. By selecting inorganic or organic acids, the differentiated debinding abilities of inorganic or organic acids can be utilized to selectively modify the charge distribution on the alumina surface, thereby optimizing the interfacial bonding strength between the adhesive network and the active components.

[0060] In some embodiments, the aging time is 6 hours to 12 hours.

[0061] The aging time is between 6 and 12 hours, allowing the binder and solvent to fully penetrate into the carrier skeleton, thereby promoting the uniform recombination of the pore structure and effectively enhancing the overall mechanical strength of the catalyst. For example, the aging time can be 6 hours, 8 hours, 10 hours, 12 hours, etc.

[0062] In some embodiments, the drying temperature is 80°C to 110°C, and the drying time is 8 hours to 24 hours.

[0063] The drying temperature is between 80℃ and 110℃, which effectively prevents phase transformation and collapse of the microstructure of the wet material during the drying process through a gradient dehydration mechanism. The drying time is between 8h and 24h to accommodate the kinetics of moisture diffusion, thereby ensuring the morphological integrity of the catalyst precursor and the permeability of the pore structure. For example, the drying temperature can be 80℃, 90℃, 100℃, 110℃, etc.; the drying time can be 8h, 12h, 16h, 20h, 24h, etc.

[0064] In some embodiments, the calcination temperature is 500℃~650℃, and the calcination time is 4h~8h.

[0065] The calcination temperature, between 500℃ and 650℃, drives the directional transformation of the metal active phase and enhances the interaction between the metal active phase and the support, thereby stabilizing the lattice oxygen species while inhibiting particle sintering. The calcination time, between 4h and 8h, matches the precursor thermal decomposition kinetics, ensuring the complete elimination of organic residues and the restructuring of the spinel phase structure, ultimately guaranteeing the high dispersion and chemical stability of the catalyst's active centers. For example, the calcination temperature can be 500℃, 550℃, 600℃, 650℃, etc.; the calcination time can be 4h, 5h, 6h, 7h, 8h, etc.

[0066] In some embodiments, the catalyst is at least one of cylindrical or spherical shapes.

[0067] The catalyst is in the shape of at least one of cylindrical or spherical. This regular geometry helps optimize fluid distribution and interparticle contact efficiency within the reactor, thereby reducing bed pressure drop while enhancing mass transfer kinetics between the gas and solid phases.

[0068] In some embodiments, the diameter of the catalyst is 1 mm to 3 mm.

[0069] The catalyst diameter is between 1 mm and 3 mm, which optimizes the diffusion path length of reactants within the particles while ensuring sufficient specific surface area. This effectively reduces the limitation of the overall reaction rate by internal diffusion resistance while maintaining high accessibility of active sites. For example, the catalyst diameter can be 1 mm, 2 mm, 3 mm, etc.

[0070] In some embodiments, the catalyst is selected from at least one of being loaded and not loaded in the gasifier; When the catalyst is selected to be packed inside the gasifier, the catalyst is located in at least one of the lower layer of biomass feedstock and the second-stage reactor.

[0071] The catalyst loading method can be flexibly selected according to the characteristics of the biomass feedstock and the requirements of process economy. It can be loaded in the gasifier or not, thereby achieving customized control of the reaction path. When loading is used in the gasifier, the catalyst can be placed in the lower layer of the biomass feedstock or in the second-stage reactor. When placed in the lower layer of the biomass feedstock, the catalyst plays an in-situ catalytic role, enhancing the reforming efficiency of by-products such as tar and hydrocarbons; when placed in the second-stage reactor, it mainly serves the function of product purification, improving the selectivity of syngas components.

[0072] Secondly, embodiments of this application provide an application of the catalyst prepared by the method described in the first aspect in the production of syngas. The catalyst is applied to the conversion of biomass carbon dioxide into syngas, and the catalyst catalyzes the conversion reaction of the syngas production. The reaction temperature of the conversion reaction is 700℃~1000℃.

[0073] The reaction temperature of the conversion reaction is between 700℃ and 1000℃, which can simultaneously activate the metal active sites of the catalyst and the oxygen migration mechanism of the support, thereby effectively driving the deep reforming of by-products such as tar and hydrocarbons, and achieving directional control of the composition ratio of syngas. For example, the reaction temperature of the conversion reaction can be 700℃, 800℃, 900℃, 1000℃, etc.

[0074] In some embodiments, the catalyst is used in the application of biomass carbon dioxide conversion to syngas, where the carbon dioxide originates from carbon dioxide captured in steel plant tail gas or conversion process tail gas.

[0075] Carbon dioxide captured from tail gas of steel plants or conversion processes using an alkanolamine solution chemical absorption method is used for the biomass carbon dioxide conversion to syngas. In this process, the catalyst plays a directed catalytic role, synergistically achieving the resource utilization of carbon dioxide and precise control of the syngas composition.

[0076] In some embodiments, the biomass carbon dioxide conversion to syngas is carried out in a reactor, which is at least one of an entrained flow bed, a fluidized bed, and a fixed bed.

[0077] The conversion of biomass carbon dioxide into syngas takes place in a reactor, which can be at least one of an entrained flow bed, a fluidized bed, or a fixed bed. By utilizing the differentiated mass transfer characteristics of different types of reactors (such as entrained flow beds, fluidized beds, or fixed beds), the mixing and contact efficiency between biomass pyrolysis products and carbon dioxide can be effectively optimized, and the dynamic renewal capability of the gas-solid reaction interface can be enhanced.

[0078] The present application is further illustrated below with reference to specific embodiments. Experimental methods in the following embodiments that do not specify specific conditions are generally determined according to national standards / industry standards / the disclosure herein; if there are no corresponding national standards / industry standards / the disclosure herein, they are performed according to generally accepted international standards, conventional conditions, or conditions recommended by the manufacturer.

[0079] Example 1 Dissolve 60g of nickel nitrate in 500mL of water and stir once for 10min to obtain a metal salt solution. 200g of alumina powder was added to the metal salt solution and stirred twice and allowed to stand. The stirring time was 0.5h and the standing time was 24h to obtain metal-loaded alumina. Metal-loaded alumina was mixed with 50g aluminum sol, 10g guar gum powder, 50g oxalic acid, 40mL nitric acid and water in sequence and aged for 6 hours to obtain wet material. The wet material is extruded, dried, and calcined sequentially. The drying temperature is 100℃ and the drying time is 12h. The calcination temperature is 550℃ and the calcination time is 6h to obtain the catalyst, which is then packed into the lower section of the gasifier.

[0080] Example 2 Dissolve 60g of nickel nitrate and 31g of cerium nitrate in 500mL of water and stir once for 15min to obtain a metal salt solution. 200g of alumina powder was added to the metal salt solution and stirred and allowed to stand twice in sequence; wherein the stirring time was 2.0h and the standing time was 24h, to obtain metal-loaded alumina; Metal-loaded alumina was mixed with 50g aluminum sol, 10g guar gum powder, 50g oxalic acid, 40mL nitric acid and water in sequence and aged for 6 hours to obtain wet material. The wet material is extruded, dried, and calcined sequentially. The drying temperature is 100℃ and the drying time is 12h. The calcination temperature is 550℃ and the calcination time is 6h to obtain the catalyst, which is then packed into the lower section of the gasifier.

[0081] Example 3 Dissolve 75g of nickel nitrate and 60g of cobalt nitrate in 800mL of water and stir once for 30min to obtain a metal salt solution. 300g of alumina powder was added to the metal salt solution and stirred twice and allowed to stand. The stirring time was 4.0h and the standing time was 24h to obtain metal-loaded alumina. Metal-loaded alumina was mixed with 100g kaolin, 20g glycerol, 100g citric acid, 40mL nitric acid and water in sequence and aged for 6 hours to obtain wet material. The wet material is extruded, dried, and calcined sequentially. The drying temperature is 100℃ and the drying time is 12h. The calcination temperature is 600℃ and the calcination time is 5h to obtain the catalyst, which is then loaded into the lower section of the gasifier.

[0082] Comparative Example 1 In the process of biomass carbon dioxide conversion to syngas, preheated carbon dioxide and biomass particles conveyed by a screw feeder flow into the gasifier in parallel, and the thermochemical conversion reaction is carried out directly without a catalyst.

[0083] Comparative Example 2 Mix 200g of alumina powder with 15g of water, then add 50g of aluminum sol, 10g of guar gum powder, 50g of oxalic acid and 40mL of nitric acid and mix and age for 6 hours to obtain wet material; The wet material is sequentially extruded, dried, and calcined; wherein the drying temperature is 100℃ and the drying time is 12h, the calcination temperature is 550℃ and the calcination time is 6h, to obtain a catalyst, which is then loaded into the lower section of the gasifier.

[0084] Results data: The experimental results of Examples 1-3 and Comparative Examples 1-2 are shown in Table 1.

[0085] Table 1

[0086] The above effect data table provides a clear comparison of the differences between various embodiments and comparative examples. The following conclusions can be drawn: Examples 1-3 and Comparative Examples 1-2 demonstrate that the use of a catalyst significantly improves the reaction rate of biomass carbon dioxide conversion. Data in Table 1 show that the CO2 conversion rate increased from 11.8% to 54.3%, an increase of 42.5 percentage points; the volume fraction of syngas (CO+H2) in the product gas increased from 67.5% to 81.9%, an increase of 14.4 percentage points; simultaneously, the volume fractions of CO2 and CH4 decreased significantly by 6.7 and 7.7 percentage points, respectively. These results indicate that the introduction of a specific catalyst can lower the activation energy and precisely control the reaction pathway, thereby effectively improving the quality of syngas in the biomass CO2 conversion products.

[0087] Appendix Figure 2 Detailed explanation: Figure 2 This is a process flow diagram for the conversion of biomass carbon dioxide to syngas, provided as an embodiment of this application. According to... Figure 2 It can be understood that the system is first purified by N2, while the catalyst loaded in the lower or second stage heating furnace of the gasifier is reduced by H2. Then, the biomass enters the gasifier through a screw feeder, and preheated carbon dioxide enters the gasifier in parallel with the biomass. Next, in the gasifier, the biomass and carbon dioxide undergo thermochemical transformation under the action of the catalyst to generate CO, H2, CH4, tar, etc. Finally, the reaction products are successively dried and purified, condensed and separated into gaseous products with syngas as the main component.

[0088] One or more technical solutions in the embodiments of the present invention have at least the following technical effects or advantages: The catalyst and process flow of this invention can flexibly control the H2 and CO ratio of syngas, thereby directly meeting the raw material requirements of different fields and downstream processes, and has a wide range of applications. Simultaneously, this process combines CO2 capture and utilization with CH4 consumption, achieving carbon emission reduction while synergistically converting it into valuable syngas resources. Furthermore, by efficiently converting low-grade biomass into high-value-added syngas, it achieves effective resource enhancement and recycling, highly aligning with the goals of circular economy development.

[0089] The above description is merely a specific embodiment of this application, enabling those skilled in the art to understand or implement this application. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of this application. Therefore, this application is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features claimed in this application.

Claims

1. A process for the preparation of a catalyst for the synthesis of syngas, characterized in that, The method includes: The metal salt is dissolved in water and stirred once to obtain a metal salt solution; Alumina powder was added to the metal salt solution and stirred and allowed to stand twice to obtain metal-loaded alumina. The alumina loaded with the metal is mixed with binder, extrusion aid, adhesive solvent and water in sequence and then aged to obtain a wet material; The wet material is sequentially extruded, dried, and calcined to obtain the catalyst.

2. The method of claim 1, wherein, The metal salt is at least one selected from rare earth metal salts, transition metal salts, and alkali metal salts; and / or, The total metal content of the metal salt solution is ≤30wt%; and / or, The content of the alumina powder is 65wt%~85wt%; and / or, The alumina powder is spherical, and the average particle size of the alumina powder is 300nm~500nm.

3. The method of claim 1, wherein, The stirring time for each stirring session is 10 to 30 minutes.

4. The method of claim 1, wherein, The secondary stirring time is 0.5h~4.0h; and / or, The settling time is ≤48h.

5. The method of claim 1, wherein, The adhesive content is 15wt%~35wt%; and / or, The binder is at least one of silica sol, alumina sol, SB powder, kaolin, clay and diatomaceous earth.

6. The method of claim 1, wherein, The mass of the extrusion aid is 2% to 7% of the total mass of the alumina powder and the binder; and / or, The extrusion aid is at least one of guar gum powder and glycerin.

7. The method of claim 1, wherein, The total mass of the adhesive solvent and the water is 30% to 80% of the total mass of the alumina powder and the binder; and / or, The adhesive solvent is at least one of nitric acid, hydrochloric acid, acetic acid, citric acid, and oxalic acid.

8. The method of claim 1, wherein, The aging time is 6h to 12h.

9. The method of claim 1, wherein, The drying temperature is 80℃~110℃, and the drying time is 8h~24h; and / or, The roasting temperature is 500℃~650℃, and the roasting time is 4h~8h.

10. The application of a catalyst prepared by the method of any one of claims 1 to 9 in the production of syngas, wherein the catalyst is applied to the conversion of biomass carbon dioxide into syngas, the catalyst catalyzes the conversion reaction of the syngas production, and the reaction temperature of the conversion reaction is 700℃ to 1000℃.

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