CeO2 loaded bimetallic catalyst as well as preparation method and application thereof

Abstract

The invention relates to a CeO2 loaded bimetallic catalyst as well as a preparation method and application thereof, and belongs to the technical field of chemical catalysts. The problems of complex preparation, high cost, harsh reaction conditions, difficulty in recovery, low efficiency, low selectivity and low stability of a common catalyst for catalyzing liquid-phase selective hydrogenation of maleic anhydride to prepare butanedioic anhydride are solved. Comprising a CeO2 carrier, a first active metal loaded on the CeO2 carrier, and a second active metal loaded on the CeO2 carrier, the mass of the CeO2 carrier is 100%, the loading capacity of the first active metal is 5-20 wt%, and the loading capacity of the second active metal is 1-10 wt%. In the preparation process, part of Ce < 4 + > is reduced into Ce < 3 + >, and Ce < 3 + > and Ce < 4 + > coexist on the surface of the catalyst, so that the cerium dioxide carrier generates a large number of oxygen vacancies, and the catalytic activity and stability of the catalyst are enhanced.

Description

Technical Field

[0001] The invention relates to a CeO2-loaded bimetallic catalyst and a preparation method and application thereof, belonging to the technical field of chemical catalysts. Background Art

[0002] Succinic anhydride, also known as succinic anhydride, has the molecular formula C4H4O3. It is an important organic synthesis intermediate and fine chemical raw material, widely used in polyester, coatings, plastics, medicine, agriculture, food, surfactants, dyes and other industrial fields.

[0003] Currently, the main methods for producing succinic anhydride include the succinic acid dehydration method and the maleic anhydride hydrogenation method. The succinic acid dehydration method involves heating succinic acid (boiling point 235°C) to dehydrate it under the catalysis of acetyl chloride, acetic anhydride, phosphorus oxychloride, phosphorus pentoxide, and the like to produce succinic anhydride. However, this method has the disadvantages of harsh reaction conditions, high production costs, and low product yields (85%-94%). Furthermore, the succinic anhydride is easily carbonized during the production process, making the process difficult to control.

[0004] Maleic anhydride hydrogenation method is divided into the melting method and the solvent dissolution catalytic method (heterogeneous catalytic hydrogenation method). The melting method does not require the addition of solvents, avoiding the consequences of using solvents that make product purification difficult and environmental pollution. However, the screening of catalyst systems and the control of reaction conditions in the melting method are technical difficulties in the hydrogenation reaction.

[0005] The heterogeneous catalytic method involves dissolving maleic anhydride in a solvent for catalytic hydrogenation. This method offers advantages such as simplicity, easy and controllable operation, low operating costs, and high product purity. It is currently a widely used industrial process for producing succinic anhydride.

[0006] Maleic anhydride molecules have one C=C and two C=O functional groups. Under certain catalytic conditions, both C=C and C=O can undergo hydrogenation reactions, but only C=C hydrogenation can produce the target product, succinic anhydride. If both C=C and C=O undergo hydrogenation reactions, the deep hydrogenation products of succinic anhydride, γ-butyrolactone (GBL) or tetrahydrofuran, can be obtained, thereby reducing the selectivity of the target product, succinic anhydride.

[0007] Therefore, the key to achieving highly selective hydrogenation of maleic anhydride to produce succinic anhydride lies in the design of a highly stable and selective catalyst that controls the reaction to the C=C double bond hydrogenation stage. Currently, the hydrogenation catalyst systems used for hydrogenation of maleic anhydride to produce succinic anhydride mainly include precious metal, copper-based, and nickel-based catalysts.

[0008] European Patent EP 0691335 discloses a method for preparing succinic anhydride by catalytic hydrogenation of maleic anhydride in the presence of a solvent. Using a Pd-based precious metal catalyst with a Pd content of 2% to 10%, and under H2 pressures of 4.0 MPa to 6.0 MPa, the yield of succinic anhydride can reach 90% to 95%. However, the catalyst has poor stability and high production costs, making industrialization difficult.

[0009] Chinese patent CN 101502802 A discloses a nickel-based catalyst with a nickel content of 13-20 wt% and a promoter content of 1%-7 wt%. It is used to hydrogenate maleic anhydride to produce succinic anhydride on a fixed bed. However, this reaction system requires high hydrogen pressure, imposes high requirements on reaction equipment, and has high production costs, making it difficult to apply in industrial applications.

[0010] U.S. Patents US 5952514 and US 5770744 disclose a catalyst formed by pressing iron and inert elements such as aluminum, silicon, titanium or iron, cobalt, nickel and carbon alloy powder for catalytic hydrogenation of maleic anhydride to prepare succinic anhydride. When the reaction temperature is 60 ℃ to 180 ℃ and the hydrogen pressure is 38 MPa, the maleic anhydride conversion is 99% and the selectivity of succinic anhydride is 98%. This process provides a method for continuously producing succinic anhydride, but the reaction conditions are harsh (hydrogen pressure is 38 MPa), and the setting and material of the reactor need to be specially required. In the catalyst, the active component content is greater than 60%, and the catalyst cost is high, which limits its large-scale application.

[0011] Chinese Patent CN 03122336.2 discloses a process for preparing succinic anhydride by hydrogenating maleic anhydride using nickel as the active component. The molar ratio of nickel, the active component, to the support is Ni:SiO2:Al2O3 = 1:(1.47-5.98):(0-3.3). The catalyst can catalyze the hydrogenation of maleic anhydride to produce succinic anhydride both in the absence of a solvent and in the presence of a solvent. The catalyst has a reduction temperature of 400°C-580°C, a reaction temperature of 120°C-180°C, a reaction time of 1-3 hours, a nickel-to-maleic anhydride molar ratio of (0.30-1.6):100, and a hydrogen pressure of 0.5 MPa-3 MPa. This catalyst uses nickel as the active component and SiO2 and Al2O3 as supports. The catalyst has acidic centers, and the reaction temperature is high during maleic anhydride hydrogenation, leading to maleic anhydride polymerization, resulting in a high product color. Furthermore, the catalyst exhibits poor stability in high-temperature, strongly acidic environments.

[0012] Therefore, it is urgent to propose a CeO2-loaded bimetallic catalyst and its preparation method and application to solve the above technical problems. Summary of the Invention

[0013] The present invention is intended to address the problems of complex catalyst preparation, high cost, harsh reaction conditions, difficulty in recovery, low efficiency, and low selectivity and stability in the liquid-phase selective hydrogenation of maleic anhydride to produce succinic anhydride, which are commonly encountered. A brief overview of the present invention is provided below to provide a basic understanding of certain aspects of the present invention. It should be understood that this overview is not an exhaustive overview of the present invention. It is not intended to identify key or important aspects of the present invention, nor is it intended to limit the scope of the present invention.

[0014] The technical solution of the present invention:

[0015] A CeO2-supported bimetallic catalyst, comprising a CeO2 carrier, a first active metal supported on the CeO2 carrier, and a second active metal supported on the CeO2 carrier;

[0016] Based on the mass of the CeO2 carrier being 100%, the loading amount of the first active metal is 5-20 wt%, and the loading amount of the second active metal is 1-10 wt%.

[0017] In some embodiments, the first active metal is nickel, preferably nickel nitrate hexahydrate.

[0018] In some embodiments, the second active metal is any one or more of cobalt, copper, or iron, preferably any one or more of cobalt nitrate hexahydrate, copper nitrate trihydrate, or ferrous sulfate heptahydrate.

[0019] In some embodiments, the average particle size of the first active metal and the second active metal particles is 5 to 20 nm, preferably 8 to 16 nm, which can achieve both high specific surface area and stability.

[0020] A method for preparing a CeO2-supported bimetallic catalyst comprises the following steps:

[0021] Step 1: CeO2 carrier, first active metal salt, second active metal salt and solvent are mixed at a stirring rate of 500-1000 r / min for 6-12 hours. After stirring, the mixture is dried at 80-120°C and then calcined at 400-500°C for 2-4 hours to obtain an oxidized catalyst;

[0022] Step 2: Place the oxidized catalyst in a H2-N2 mixed atmosphere and reduce it at 350-550°C for 1-5h to obtain a CeO2-supported bimetallic catalyst.

[0023] In some embodiments, ultrasound can be used to assist the impregnation before stirring, with the ultrasound frequency being 40 kHz and the ultrasound time being 30 min.

[0024] In some embodiments, the calcination process is carried out in air or an inert atmosphere (N2, Ar), preferably in air, with a heating rate of 1-5°C / min.

[0025] In some embodiments, the reduced catalyst may be cooled to room temperature in an inert atmosphere and subjected to a surface passivation treatment.

[0026] In some embodiments, the CeO2 carrier has a mesoporous structure with a specific surface area of 50-150 m 2 / g, and is pre-treated with acid or modified by doping with Zr elements to enhance metal dispersion.

[0027] In some embodiments, the volume flow ratio of H2:N2 in the H2-N2 mixed gas is 1:1-5.

[0028] Application of CeO2-supported bimetallic catalyst prepared according to any of the above methods in the hydrogenation of maleic anhydride to synthesize succinic anhydride.

[0029] Preferably: the CeO2-loaded bimetallic catalyst and maleic anhydride solution are added to a high-pressure reactor, the reaction temperature of the high-pressure reactor is 120-240°C, the hydrogen pressure is 2-6 MPa, the reaction time is 0.5-4h, the content of maleic anhydride in the maleic anhydride solution is 5-10wt%, the solution is one of tetrahydrofuran, 1,4-dioxane or cyclohexane, and the amount of CeO2-loaded bimetallic catalyst is 0.1-0.6g catalyst / g maleic anhydride.

[0030] The present invention has the following beneficial effects:

[0031] During the preparation process of the present invention, part of Ce 4+ Reduction to Ce 3+ , and Ce 3+ and Ce 4+ Coexisting on the surface of the catalyst, the ceria support generates a large number of oxygen vacancies, thereby enhancing the catalytic activity and stability of the catalyst;

[0032] In the present invention, the synergistic effect between the bimetallic particles makes the active metal particles uniformly dispersed and not easily aggregated. The catalyst has the advantages of high reactivity, good selectivity, and strong stability in the selective catalytic liquid-phase hydrogenation reaction of maleic anhydride due to its special and stable coordination environment and the synergistic effect between the supported bimetallic particles.

[0033] The CeO2-loaded bimetallic catalyst provided by the present invention performs hydrogenation reaction, and the yield of succinic anhydride obtained is high, and the selectivity is above 90%, and there is no attenuation after 5 cycles, and the catalyst has excellent cycle stability. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 1 is the X-ray diffraction pattern of the CeO2-based catalyst loaded with nickel and cobalt particles prepared in Example 1. DETAILED DESCRIPTION

[0035] To make the objectives, technical solutions, and advantages of the present invention more clearly apparent, the present invention is described below using specific embodiments shown in the accompanying drawings. However, it should be understood that these descriptions are merely illustrative and are not intended to limit the scope of the present invention. In addition, in the following description, descriptions of well-known structures and technologies are omitted to avoid unnecessary confusion of the concepts of the present invention.

[0036] In view of the problems in the prior art of catalyzing the liquid-phase selective hydrogenation of maleic anhydride to produce succinic anhydride, such as complex preparation, high cost, harsh reaction conditions, difficulty in recovery, low efficiency, low selectivity and low stability, the present invention provides a CeO2-supported bimetallic catalyst, referred to as NiM / CeO2, which includes a CeO2 support and an active metal supported on the CeO2 support (wherein M represents a specific second active metal element).

[0037] Example 1

[0038] A method for preparing a NiM / CeO2 catalyst comprises the following steps:

[0039] Step 1: Disperse 100 mg of CeO2 in 2.5 mL of aqueous solution, add 25 mg of nickel nitrate hexahydrate and 2 mg of cobalt nitrate hexahydrate, and stir at 60 ° C for 24 hours at a speed of 500 r / min; dry at 100 ° C, and finally calcine the obtained intermediate mixture at 400 ° C in a muffle furnace for 3 hours at a heating rate of 5 ° C / min, and then cool to room temperature;

[0040] Step 2: The catalyst was reduced in a 25V% H2-75V% N2 mixed gas atmosphere at a gas flow rate of 40 ml / min, heated to 400°C at a rate of 5°C / min for 2 h to obtain a NiM / CeO2 catalyst.

[0041] During the implementation of Example 1 of the present invention, a hydrogenation experiment was conducted to obtain the following experimental results:

[0042] 1. X-ray diffraction was used to characterize the CeO2-based catalyst loaded with nickel and cobalt particles, and the following results were obtained: Figure 1 The X-ray diffraction pattern shown. Figure 1 It can be seen that the CeO2-based catalyst loaded with nickel and cobalt particles prepared in Example 1 of the present invention has no obvious metal diffraction peaks, confirming that it is in the state of nickel single atoms and platinum nanoparticles (the particles are too small to show crystal diffraction peaks).

[0043] 2. The CeO2-based catalyst loaded with nickel and cobalt particles was used as a catalyst for the hydrogenation reaction of maleic anhydride and its performance was tested. The specific process is as follows: In the hydrogen hydrogenation process, 2g of maleic anhydride, 0.1g of the CeO2-based catalyst loaded with nickel and cobalt particles prepared in Example 1 of the present invention, and 40mL of 1,4-dioxane were added to a high-pressure reactor, and nitrogen was introduced to 1MPa. This operation was performed three times in succession to evacuate the gas in the reactor. Hydrogen was then introduced to 4MPa, the reactor was closed, the reaction temperature was set to 160°C and the reaction time was 3h, and the reaction was cooled to room temperature after the reaction was completed. The maleic anhydride hydrogenation reaction has high activity, and the selectivity of succinic anhydride is greater than 90%.

[0044] Example 2

[0045] The difference from Example 1 is that 50 mg of nickel nitrate hexahydrate is used as the first active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0046] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0047] Example 3

[0048] The difference from Example 1 is that 75 mg of nickel nitrate hexahydrate is used as the first active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0049] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0050] Example 4

[0051] The difference from Example 1 is that 100 mg of nickel nitrate hexahydrate is used as the first active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0052] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0053] Example 5

[0054] The difference from Example 1 is that 0.5 mg of cobalt nitrate hexahydrate is used as the second active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0055] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0056] Example 6

[0057] The difference from Example 1 is that 3.5 mg of cobalt nitrate hexahydrate is used as the second active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0058] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0059] Example 7

[0060] The difference from Example 1 is that 5 mg of cobalt nitrate hexahydrate is used as the second active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0061] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0062] Example 8

[0063] The difference from Example 1 is that 3 mL of water is used to disperse CeO2, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0064] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0065] Example 9

[0066] The difference from Example 1 is that the rotation speed is changed to 1000 r / min and stirring is carried out for 12 hours. The remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the second active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0067] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0068] Example 10

[0069] The difference from Example 1 is that the drying temperature is set to 120°C after stirring and centrifugation, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the second active metal salt, the impregnation time, the calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0070] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0071] Example 11

[0072] The difference from Example 1 is that the calcination reduction temperature is 450°C for 2 hours, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the second active metal salt, the impregnation time, the drying conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and cobalt particles.

[0073] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0074] Example 12

[0075] The difference from Example 1 is that 1.18 mg of copper nitrate trihydrate is used as the second active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and copper particles.

[0076] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0077] Example 13

[0078] The difference from Example 1 is that 2 mg of ferrous sulfate heptahydrate is used as the second active metal salt, and the remaining steps and parameters (including the amount of carrier CeO2, the type and amount of the first active metal salt, the impregnation time, the drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with nickel and iron particles.

[0079] The reaction performance test was the same as that in Example 1. The maleic anhydride hydrogenation reaction had high activity and the selectivity of succinic anhydride was greater than 90%.

[0080] Comparative Example 1

[0081] The difference from Example 1 is that only 50 mg of nickel nitrate hexahydrate is used as the first active metal salt, and no second active metal salt is added. The remaining steps and parameters (including the amount of carrier CeO2, impregnation time, drying / calcination / reduction conditions, etc.) are consistent with Example 1, and the obtained material is a CeO2-based catalyst loaded with nickel particles.

[0082] The detection method was the same as that of Example 1, and it was found that the catalytic activity was 80% of that of Example 1, and the selectivity of succinic anhydride was greater than 90%.

[0083] Comparative Example 2

[0084] The difference from Example 1 is that only 2 mg of cobalt nitrate hexahydrate is used as the second active metal salt, and the first active metal salt is not added. The remaining steps and parameters (including the amount of carrier CeO2, impregnation time, drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with cobalt particles.

[0085] The detection method was the same as that of Example 1, and it was found that the catalytic activity was 20% of that of Example 1, and the selectivity of succinic anhydride was greater than 90%.

[0086] Comparative Example 3

[0087] The difference from Example 1 is that only 1.18 mg of copper nitrate hexahydrate is used as the second active metal salt, and the first active metal salt is not added. The remaining steps and parameters (including the amount of carrier CeO2, impregnation time, drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with copper particles.

[0088] The detection method was the same as that of Example 1, and it was found that the catalytic activity was 18% of that of Example 1, and the selectivity of succinic anhydride was greater than 90%.

[0089] Comparative Example 4

[0090] The difference from Example 1 is that only 2 mg of ferrous sulfate heptahydrate is used as the second active metal salt, and the first active metal salt is not added. The remaining steps and parameters (including the amount of carrier CeO2, impregnation time, drying / calcination / reduction conditions, etc.) are consistent with Example 1. The obtained material is a CeO2-based catalyst loaded with iron particles.

[0091] The detection method was the same as that of Example 1, and it was found that the catalytic activity was 10% of that of Example 1, and the selectivity of succinic anhydride was greater than 90%.

[0092] In the present invention, the CeO2 carrier is cheap and stable. The present invention preferably uses a flaky CeO2 carrier with a large specific surface area, which can provide more metal growth binding sites, making it easier to form active metal particles later.

[0093] Excessive loading of the active metal can cause it to aggregate, reducing its effective catalytic area and hindering subsequent practical applications. Therefore, in the present invention, based on the mass of the CeO2 carrier as 100%, the loading of the first active metal Ni is 5-20wt%, preferably 10-15wt%, and the loading of the second active metal is 1-10wt%, preferably 3-7wt%. The present invention does not particularly limit the ratio of the first active metal to the second active metal particles, as long as the above loading range is met.

[0094] In the present invention, the above-mentioned active metal particles can be evenly dispersed and are not easily aggregated. The catalyst has the advantages of high reaction activity, good selectivity, and strong stability in the selective catalytic liquid-phase hydrogenation reaction of maleic anhydride due to its special and stable coordination environment and the synergistic effect between the loaded bimetallic particles.

[0095] It should be noted that in the above embodiments, as long as the technical solutions are not contradictory, they can be permuted and combined. Those skilled in the art can exhaust all possibilities based on the mathematical knowledge of permutations and combinations. Therefore, the present invention will no longer describe the technical solutions after permutations and combinations one by one, but it should be understood that the technical solutions after permutations and combinations have been disclosed by the present invention.

[0096] The foregoing description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Those skilled in the art will readily appreciate that various modifications and variations of the present invention are possible. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention are intended to be within the scope of protection of the present invention.

Claims

1. A CeO2-supported bimetallic catalyst, characterized in that: The CeO2-supported bimetallic catalyst consists of a CeO2 carrier, a first active metal supported on the CeO2 carrier, and a second active metal supported on the CeO2 carrier; Based on the mass of the CeO2 carrier being 100%, the loading amount of the first active metal is 5-20 wt%, and the loading amount of the second active metal is 1-10 wt%.

2. A CeO2-supported bimetallic catalyst according to claim 1, characterized in that: The first active metal is nickel, and the second active metal is any one or more of cobalt, copper or iron.

3. A CeO2-supported bimetallic catalyst according to claim 1 or 2, characterized in that: The average particle size of the first active metal and the second active metal particles is 5 to 20 nm.

4. A method for preparing a CeO2-supported bimetallic catalyst, characterized in that: The steps include: Step 1: CeO2 carrier, first active metal salt, second active metal salt and solvent are mixed and stirred for 6 to 12 hours. After stirring, the mixture is dried at 80 to 120°C and then calcined at 400 to 500°C for 2 to 4 hours to obtain an oxidized catalyst; Step 2: Place the oxidized catalyst in a H2-N2 mixed atmosphere and reduce it at 350-550°C for 1-5h to obtain a CeO2-supported bimetallic catalyst.

5. The method for preparing a CeO2-supported bimetallic catalyst according to claim 4, wherein: The mass volume ratio of the CeO2 carrier, the first active metal salt, the second active metal salt and the solvent is 100 mg: 5-20 mg: 1-10) mg: 2.5-5) mL.

6. The method for preparing a CeO2-supported bimetallic catalyst according to claim 4, wherein: The stirring rate is 500-1000 r / min, and the calcination is carried out in an air atmosphere.

7. The method for preparing a CeO2-supported bimetallic catalyst according to claim 4, wherein: The volume flow ratio of H2:N2 in the H2-N2 mixed gas is 1:1-5.

8. Use of the CeO2-supported bimetallic catalyst prepared by the method according to any one of claims 1 to 7 in the synthesis of succinic anhydride by hydrogenation of maleic anhydride.

9. The use according to claim 8, characterized in that: The CeO2-loaded bimetallic catalyst and maleic anhydride solution are added to a high-pressure reactor. The reaction temperature of the high-pressure reactor is 120-240°C, the hydrogen pressure is 2-6 MPa, and the reaction time is 0.5-4 h. The content of maleic anhydride in the maleic anhydride solution is 5-10 wt%, and the solution is one of tetrahydrofuran, 1,4-dioxane or cyclohexane. The amount of CeO2-loaded bimetallic catalyst is 0.1-0.6 g catalyst / g maleic anhydride.

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