A catalyst carrier, a catalyst, and a preparation method and application thereof

Abstract

The present application provides a catalyst carrier, a catalyst and a preparation method and application thereof, and belongs to the field of catalysts, and solves the problem of easy peeling and abrasion of the surface catalytic active component of a coating type carrier catalyst in the prior art.The catalyst carrier comprises a porous support body and a carrier material for carrying an active component filled in the surface pores of the porous support body, and the filling thickness of the carrier material is 5% to 30% of the radius of the porous support body, preferably 10% to 30%.The present application avoids the peeling of the active component loading layer from the support body, reduces the exposure of the active component on the outer surface of the catalyst particles, and thus reduces the loss of the active component.

Description

Technical Field

[0001] This invention belongs to the field of catalysts, specifically relating to a catalyst support, a catalyst, its preparation method, and its application. Background Technology

[0002] In existing coated catalysts, the catalytically active components are distributed on the surface of the catalyst, exposed to the elements. During transport, loading, and use, friction between catalyst particles, collisions between the catalyst and equipment, and prolonged exposure to reactant gases inevitably cause the coating to peel off and wear down. This peeling and wear leads to the loss of active components, especially expensive platinum-based metals such as platinum, which not only affects catalyst performance but also results in resource and economic losses. Summary of the Invention

[0003] Therefore, the technical problem to be solved by the present invention is to overcome the defects of easy peeling and wear of catalytic active components on the surface of coated catalysts in the prior art, which affects the catalyst performance and causes resource and economic losses. Thus, the present invention provides a catalyst support, a catalyst, a preparation method thereof, and an application thereof.

[0004] To this end, the present invention provides the following technical solution.

[0005] In a first aspect, the present invention provides a catalyst support comprising a porous support and a support material for carrying an active component, the support material being filled in the pores on the surface of the porous support, wherein the filling thickness of the support material is 5% to 30% of the radius of the porous support, preferably 10% to 30%.

[0006] All the supporting material is distributed within the porous support body near the surface, with no supporting material on the outer surface. In the field of saturated hydrocarbon dehydrogenation, especially in the selective oxidation of hydrogen in ethylbenzene dehydrogenation, coated catalysts exhibit significantly better performance than catalysts with uniform composition. This invention controls the thickness of the active component supported layer to 5%–30%, maintaining a shell-core structure in the overall catalyst structure. If the thickness of the active component supported layer is too large, it will no longer be a shell-core structure, reducing catalyst selectivity; if the thickness is too small, the amount of active component loaded will be insufficient, reducing catalyst reactivity. Therefore, the thickness of the active component supported layer is controlled to 5%–30%. This invention controls the thickness of the unsupported layer within the support body by controlling the amount of pore spacer used, thereby controlling the thickness of the active component supported layer.

[0007] According to some embodiments of the present invention, the porosity of the porous support is 50% to 90%; and / or the porous support is at least one of α-alumina, silicon carbide, spinel, mullite and cordierite, preferably cordierite; and / or the porous support is a spherical porous support or a strip-shaped porous support; preferably a spherical porous support.

[0008] If the porosity is too high, the strength of the porous support will be too low, making it difficult to meet the requirements for industrial catalyst use; if the porosity is too low, the material carried in the prepared support will be too small, and the loading of active components that meet the requirements for use cannot be obtained when preparing the corresponding catalyst.

[0009] According to some embodiments of the present invention, the porous support is at least one of α-alumina, silicon carbide, spinel, mullite and cordierite, preferably cordierite;

[0010] According to some embodiments of the present invention, the average particle size of the catalyst support is 2 to 10 mm, and the particle size range of the porous support is 2 to 10 mm.

[0011] The supporting material is at least one of γ-alumina, δ-alumina, θ-alumina, and molecular sieves, preferably γ-alumina. For example, the molecular sieve may be ZSM-5 molecular sieve or SAPO34 molecular sieve.

[0012] Secondly, the present invention provides a method for preparing a catalyst support, comprising the following steps:

[0013] Step 1: Impregnate the porous support with a solution containing a pore-filling agent, remove it and dry it under positive pressure to obtain a support containing a pore-filling agent;

[0014] Step 2: Immerse the support containing the pore spacer in the suspension of the carrier material, remove it, and then dry and calcine it to obtain the catalyst support.

[0015] In step 1, the pore spacer solution is prepared by dissolving the pore spacer in a solvent; the mass percentage of the pore spacer in the pore spacer solution is more than 20%, preferably, the pore spacer solution is a saturated solution, which can reduce the amount of solvent used, thereby reducing the time required to remove the solvent and shortening the preparation cycle.

[0016] According to some embodiments of the present invention, the pore-filling agent is selected from one or more of paraffin wax, palmitic acid, stearic acid, eicosanoic acid, ligninic acid, cetyl alcohol, dodecyl alcohol, and triglycerides. Suitable paraffin waxes for use in the present invention can be any of high-melting-point, medium-melting-point, and low-melting-point paraffin waxes.

[0017] According to some embodiments of the present invention, the solvent is a benign solvent for pore spacers, preferably at least one of alcohol solvents, ether solvents and halogenated hydrocarbon solvents, more preferably at least one of C1-C4 alcohol compounds, C1-C4 ether compounds and C2-C6 halogenated hydrocarbons, and even more preferably at least one of ethanol, diethyl ether and chloroform.

[0018] According to some embodiments of the present invention, the immersion time of the porous support in the pore spacer solution is 5 minutes to 1 hour. If the time is too short, the pore spacer cannot be completely immersed in the support. If the time is too long, it has no positive effect on changing the performance of the support and catalyst, and prolongs the preparation cycle.

[0019] According to some embodiments of the present invention, when the porous support is immersed in the pore spacer solution, ultrasonication is performed simultaneously to help remove air from the support and allow the pore spacer to be completely immersed in the support.

[0020] According to some embodiments of the present invention, in step 1, the pressure of positive pressure drying is 0.15–3 MPa, preferably 0.2–1 MPa. Under positive pressure drying conditions, the pore-filling agent will not migrate to the surface of the support as the solvent evaporates, but will occupy a portion of the support core, thereby achieving the function of pore filling.

[0021] According to some embodiments of the present invention, in step 1, the temperature of positive pressure drying is 80-150°C, and the drying time is 0.5-4 hours; during the positive pressure drying process, nitrogen gas is continuously introduced to purge and remove the solvent of the pore spacer solution.

[0022] According to some embodiments of the present invention, the method for preparing the suspension of the carrier material in step 2 includes: adding the carrier material to water and stirring to disperse it, then adding aluminum sol and continuing to stir to obtain a suspension of the carrier material.

[0023] According to some embodiments of the present invention, the solid-liquid mass ratio of the carrier material of the suspension to water is 1:5 to 1:1.

[0024] According to some embodiments of the present invention, in step 2, the immersion time of the support containing the pore spacer in the suspension is 5 minutes to 1 hour. If the time is too short, the suspension cannot be completely immersed in the support. If the time is too long, it will not have a positive effect on changing the performance of the support and catalyst, and will prolong the preparation cycle.

[0025] In step 2, the specific steps of drying and calcining are as follows: first, dry at 80-150℃ for 1-12 hours to remove water from the suspension; then calcin at 400-1000℃ for 2-8 hours to remove the pore spacer and at the same time, firmly bond the bearing material to the support.

[0026] Thirdly, the present invention provides a catalyst comprising the catalyst support described above or the catalyst support obtained by the preparation method described above, and a platinum group metal active component supported on the support material.

[0027] According to some embodiments of the present invention, the platinum group metal active component is one or more selected from ruthenium, rhodium, osmium, platinum and palladium;

[0028] Preferably, the content of the platinum group metal active component is 0.01-5.0% of the catalyst weight based on elemental metal, more preferably 0.05-1.0%. In this invention, platinum group metals are the main active components, and their content is a key factor affecting catalyst activity. Too little content results in insufficient catalyst activity; too much content increases catalyst cost and also hinders platinum group metal particle dispersion, which is also detrimental to catalytic activity. The platinum group metal active component content of this invention balances catalytic activity and catalyst economy.

[0029] Fourthly, the present invention provides a method for preparing a catalyst, comprising the following steps:

[0030] The catalyst support was impregnated in an aqueous solution containing platinum group metal element compounds, then removed, dried, and calcined.

[0031] According to some embodiments of the present invention, the platinum group metal compound is at least one selected from platinum chloride, ruthenium chloride, rhodium chloride, osmium chloride, palladium chloride, chloroplatinic acid, and chloropalladium acid, preferably chloroplatinic acid.

[0032] According to some embodiments of the present invention, the catalyst is prepared by an equal-volume impregnation method. Based on the loading of the platinum group metal active component of the catalyst, the required amount of platinum group metal element compound is calculated and weighed, dissolved in water, and prepared into an aqueous solution of the corresponding platinum group metal element compound.

[0033] According to some embodiments of the present invention, drying and calcination include: first drying at a temperature of 80–150°C for 1–12 hours to remove solvent water, and then calcining at a temperature of 550–800°C for 1–6 hours to decompose the platinum group metal element compound into platinum group active components, thereby achieving the reaction performance of a catalyst.

[0034] Fifthly, the present invention provides the application of a catalyst or a catalyst prepared according to the above preparation method in the dehydrogenation of saturated hydrocarbons to produce unsaturated hydrocarbons, preferably, the saturated hydrocarbon is ethylbenzene and the unsaturated hydrocarbon is styrene.

[0035] In a sixth aspect, the present invention provides a method for producing unsaturated hydrocarbons by dehydrogenation of saturated hydrocarbons, comprising subjecting hydrogen produced by dehydrogenation of saturated hydrocarbons to a selective oxidation reaction in the presence of a catalyst;

[0036] Preferably, the conditions for the selective oxidation reaction include a reaction temperature of 520-650℃, a reaction pressure of 20-200 kPa, and a liquid hourly space velocity of 0.1-10 h⁻¹. -1 .

[0037] The technical solution of this invention has the following advantages:

[0038] 1. The catalyst support provided by the present invention has an active component loading layer embedded inside the support, which avoids the active component loading layer peeling off from the support and reduces the exposure of the active component on the outer surface of the catalyst particles, thereby reducing the loss of platinum group metal active components.

[0039] 2. The catalyst support preparation method provided by the present invention uses a pore spacer to occupy part of the core of the porous support, so that the subsequently introduced support material can only penetrate into a certain area near the surface of the porous support, thereby obtaining a catalyst that maintains a shell-core structure in the overall structure, and thus the corresponding catalyst maintains good reaction performance. Attached Figure Description

[0040] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0041] Figure 1 This is a scanning electron microscope (SEM) image of the catalyst support cross-section in Example 1 of this invention;

[0042] Figure 2 This is a partial magnified scanning electron microscope image of the catalyst support cross-section in Example 1 of the present invention;

[0043] Figure 3 This is a scanning electron microscope image of the cross-section of the catalyst support in Comparative Example 1 of the present invention. Detailed Implementation

[0044] The following embodiments are provided to better understand the present invention and are not limited to the preferred embodiments described. They do not constitute a limitation on the content and scope of protection of the present invention. Any product that is the same as or similar to the present invention, derived by any person under the guidance of the present invention or by combining the features of the present invention with other prior art, falls within the protection scope of the present invention.

[0045] For experiments not specifically described in the examples, the procedures or conditions should be followed according to the conventional experimental procedures described in the literature in this field. Reagents or instruments whose manufacturers are not specified are all commercially available conventional reagent products.

[0046] Example 1

[0047] (1) Preparation of catalyst support

[0048] Step 1: Dissolve 100g of stearic acid in 37g of ethanol to prepare a stearic acid solution. Immerse 100g of cordierite particles with a particle size of 4.5mm and a porosity of 70% in the solution and sonicate at a working frequency of 50Hz for 10 minutes. Remove and filter. Place the filtered cordierite particles in a pressure-resistant container and continuously purge with nitrogen gas, controlling the pressure inside the container at 0.2MPa. Heat the container to 120℃ to remove the ethanol. After 2 hours, remove the particles to obtain cordierite particles containing stearic acid.

[0049] Step 2: Take 45g of γ-alumina powder sieved through a 100-mesh sieve and add it to 100mL of water, stirring to disperse. Then add 2.5g of aluminum sol (20% by mass, based on alumina) and stir for 1 hour to obtain a γ-alumina suspension. Immerse stearic acid-containing cordierite particles in the suspension, remove and filter after 30 minutes. Then dry at 100℃ for 3 hours, and then calcine at 650℃ for 6 hours. A catalyst support with γ-alumina embedded in a cordierite support and layered near the spherical surface is obtained, with the γ-alumina layer thickness being 10% of the particle radius. A scanning electron microscope image of the catalyst support cross-section is shown below. Figure 1 and Figure 2 .

[0050] (2) Catalyst preparation

[0051] Chloroplatinic acid was dissolved in water to prepare a platinum content solution of 30.2 mg / mL. The catalyst support obtained above was immersed in a chloroplatinic acid solution of equal volume, then dried at 120°C for 4 hours, and then calcined at 600°C for 6 hours. This yielded catalyst A, in which platinum was distributed in layers on γ-alumina near the spherical surface within a cordierite support. Elemental analysis showed that platinum accounted for 0.21% of the catalyst by mass.

[0052] The wear rate of catalyst A was determined to be 0.16% according to the method in standard HG / T 2976-1999. The powder collected during the wear rate test was analyzed by elemental analysis, and the mass fraction of platinum in the powder was determined to be 0.54%. The loss rate of the active component platinum was 0.41%.

[0053] Example 2

[0054] (1) Preparation of catalyst support

[0055] Step 1: Dissolve 52g of No. 30 low-melting-point paraffin wax in 52g of diethyl ether to prepare a paraffin wax solution. Immerse 100g of cordierite particles with a particle size of 4.5mm and a porosity of 55% in the solution and sonicate at a working frequency of 50Hz for 10 minutes. Remove and filter. Place the filtered cordierite particles in a pressure-resistant container and continuously purge with nitrogen gas, controlling the pressure inside the container at 2MPa. Heat the container to 80℃ to remove the diethyl ether. After 4 hours, remove the particles to obtain cordierite particles containing paraffin wax.

[0056] Step 2: Take 80g of δ-alumina powder (screened through a 100-mesh sieve) and add it to 100mL of water, stirring to disperse. Then add 5g of aluminum sol (20% by mass, based on alumina content), and stir for 1 hour to obtain a δ-alumina suspension. Immerse paraffin-containing cordierite particles in the suspension, and filter after 60 minutes. Then dry at 80℃ for 12 hours, followed by calcination at 800℃ for 4 hours. This yields a catalyst support in which δ-alumina is embedded in a cordierite support and layered near the spherical surface, with the δ-alumina layer thickness being 20% ​​of the particle radius.

[0057] (2) Catalyst preparation

[0058] Platinum chloride was dissolved in water to prepare a solution with a platinum content of 89.1 mg / mL. The obtained catalyst support was immersed in a platinum chloride solution of equal volume, then dried at 150°C for 1 hour, and then calcined at 650°C for 3 hours. This yielded catalyst B, in which platinum was distributed in layers on δ-alumina near the spherical surface within a cordierite support. Elemental analysis showed that platinum accounted for 0.97% of the catalyst by mass.

[0059] The wear rate of catalyst B was determined to be 0.10% according to the standard HG / T 2976-1999. The powder collected during the wear rate test was analyzed by elemental analysis, and the mass fraction of platinum in the powder was found to be 2.0%. The loss rate of the active component platinum was 0.21%.

[0060] Example 3

[0061] (1) Preparation of catalyst support

[0062] Step 1: Dissolve 50 g of dodecanol in 96 g of ethanol to prepare a dodecanol solution. Immerse 100 g of α-alumina particles with a particle size of 3.0 mm and a porosity of 90% in the solution and sonicate at a working frequency of 50 Hz for 10 minutes. Filter the solution. Place the filtered α-alumina particles in a pressure-resistant container and continuously purge with nitrogen gas, controlling the pressure inside the container at 0.5 MPa. Heat the container to 150 °C to remove the ethanol. After 1 hour, remove the particles to obtain α-alumina particles containing dodecanol.

[0063] Step 2: Take 60g of θ-alumina powder sieved through a 100-mesh sieve and add it to 100mL of water, stirring to disperse. Then add 5g of aluminum sol (10% by mass, based on alumina content), and stir for 1 hour to obtain an θ-alumina suspension. Immerse the dodecanol-containing α-alumina particles in the suspension, remove and filter after 15 minutes. Then dry at 100℃ for 10 hours, followed by calcination at 900℃ for 3 hours. This yields a catalyst support in which θ-alumina is embedded within an α-alumina support in a layered distribution near the spherical surface, with the θ-alumina layer thickness being 30% of the particle radius.

[0064] (2) Catalyst preparation

[0065] Palladium chloride was dissolved in hydrochloric acid aqueous solution to prepare a palladium concentration of 18.5 mg / mL. The obtained catalyst support was immersed in an equal volume of palladium chloride solution, then dried at 100°C for 6 hours, and then calcined at 550°C for 5 hours. This yielded catalyst C, in which palladium is distributed in layers on δ-alumina near the spherical surface within an α-alumina support. Elemental analysis showed that platinum constituted 0.5% of the catalyst by mass.

[0066] The wear rate of catalyst C was determined to be 0.18% according to the standard HG / T 2976-1999. The powder collected during the wear rate test was analyzed by elemental analysis, and the mass fraction of palladium in the powder was determined to be 0.76%. The loss rate of the active component palladium was 0.27%.

[0067] Comparative Example 1

[0068] A γ-alumina suspension was prepared using the same method as in Example 1. The γ-alumina was then coated onto the outer surface of cordierite particles by spraying until the coating thickness was 10% of the cordierite particle radius, thus obtaining a catalyst support in which γ-alumina was distributed in layers on the outer surface of cordierite.

[0069] The cross-sectional scanning electron microscope image of the catalyst support in Comparative Example 1 is shown below. Figure 3 Using the same preparation method and conditions as in Example 1, chloroplatinic acid was dissolved in water to prepare a solution, and then platinum was loaded onto a support to obtain catalyst A', in which platinum is distributed in layers on the outer surface of cordierite and on γ-alumina. Elemental analysis showed that platinum accounted for 0.21% of the catalyst by mass.

[0070] The wear rate of catalyst A' was 0.52%. The powder collected during the wear rate test was analyzed by elemental analysis, and the mass fraction of platinum in the powder was determined to be 0.78%. The loss rate of the active component, platinum, was 1.93%.

[0071] Application Example 1

[0072] The catalysts prepared in Example 1 and Comparative Example 1 were used in the production of styrene by dehydrogenation of ethylbenzene, and the specific processes are shown below.

[0073] The hydrogen production process for the catalytic selective oxidation of saturated aromatic hydrocarbon ethylbenzene to unsaturated aromatic hydrocarbon styrene was carried out in a stainless steel reaction tube with a catalyst loading of 30 mL. The reactant composition consisted of styrene 2.4% (molar composition), ethylbenzene 5.4%, benzene and toluene 0.08%, hydrogen 2.4%, oxygen 1.1%, nitrogen 0.11%, and water 88.51%. The reaction temperature was 580 °C, the reaction pressure was 100 kPa, and the space velocity was 3 h⁻¹. -1 The result obtained is:

[0074] Table 1 shows the evaluation results using the catalysts from Example 1 and Comparative Example 1.

[0075] catalyst Hydrogen conversion rate % Oxygen conversion rate % Oxygen selectivity % A 81.3 99.8 89.1 A’ 80.9 99.8 88.7

[0076] As shown in Table 1, the catalyst performance of this invention is comparable to, or even slightly superior to, existing coated carrier catalysts. This invention significantly reduces the loss rate of active catalyst components while ensuring catalyst performance, thus solving the problem of coating peeling and wear.

[0077] Any numerical value mentioned in this invention, if there is only a two-unit interval between any minimum and any maximum value, includes all values ​​that increase by one unit each time from the minimum to the maximum value. For example, if the amount of a component, or the value of a process variable such as temperature, pressure, or time, is stated as 50-90, in this specification it means specifically listing values ​​such as 51-89, 52-88… and 69-71 and 70-71, etc. For non-integer values, it may be appropriately considered that a unit is 0.1, 0.01, 0.001, or 0.0001. These are merely some specifically specified examples. In this application, in a similar manner, all possible combinations of numerical values ​​between the listed minimum and maximum values ​​are considered to have been disclosed.

[0078] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.

Claims

1. A catalyst support, characterized in that, It includes a porous support and a carrier material filling the pores on the surface of the porous support for carrying the active component, wherein the filling thickness of the carrier material is 5% to 30% of the radius of the porous support. The porous support is at least one of α-alumina, silicon carbide, spinel, mullite, and cordierite. The supporting material is at least one of γ-alumina, δ-alumina, θ-alumina, and molecular sieve. The method for preparing a catalyst support includes the following steps: Step 1: Impregnate the porous support with a solution containing a pore-filling agent, remove it and dry it under positive pressure to obtain a support containing a pore-filling agent; Step 2: Immerse the support containing the pore spacer in a suspension containing the carrier material, then remove it and sequentially dry and calcine it to obtain the catalyst support. In step 1, the pore-filling agent is selected from one or more of paraffin wax, palmitic acid, stearic acid, eicosanoic acid, ligninic acid, cetyl alcohol, dodecyl alcohol, and triglycerides.

2. The catalyst support according to claim 1, characterized in that, The filling thickness of the bearing material is 10% to 30% of the radius of the porous support; and / or the porosity of the porous support is 50% to 90%; and / or the porous support is a spherical porous support or a strip-shaped porous support.

3. The catalyst support according to claim 2, characterized in that, The porous support is cordierite; and / or the porous support is a spherical porous support.

4. The catalyst support according to claim 1, characterized in that, The supporting material is γ-alumina.

5. The catalyst support according to any one of claims 1-4, characterized in that, The average particle size of the catalyst support is 2~10 mm.

6. A method for preparing a catalyst support according to any one of claims 1-5, characterized in that, Includes the following steps: Step 1: Impregnate the porous support with a solution containing a pore-filling agent, remove it and dry it under positive pressure to obtain a support containing a pore-filling agent; Step 2: Immerse the support containing the pore spacer in a suspension containing the carrier material, remove it, and then dry and calcine it in sequence to obtain the catalyst carrier.

7. The method for preparing the catalyst support according to claim 6, characterized in that, The solution containing the pore-filling agent also includes a solvent, which is a benign solvent for the pore-filling agent. And / or in the solution containing the pore spacer, the mass percentage of the pore spacer is 20% or more.

8. The method for preparing the catalyst support according to claim 7, characterized in that, The solvent is at least one of alcohol solvents, ether solvents, and halocarbon solvents; And / or the solution containing a pore-filling agent is a saturated solution.

9. The method for preparing the catalyst support according to claim 8, characterized in that, The solvent is at least one of C1-C4 alcohols, C2-C4 ethers, and C1-C6 halogenated hydrocarbons.

10. The method for preparing the catalyst support according to claim 9, characterized in that, The solvent is at least one of ethanol, diethyl ether, and chloroform.

11. The method for preparing the catalyst support according to claim 6, characterized in that, In step 1, the pressure of positive pressure drying is 0.15~3MPa; the temperature is 80~150℃; and / or in step 2, the calcination conditions are calcination at 400~1000℃ for 2~8 hours.

12. The method for preparing the catalyst support according to claim 11, characterized in that, In step 1, the pressure for positive pressure drying is 0.2~1MPa.

13. A catalyst, characterized in that, It includes the catalyst support as described in any one of claims 1-5 or the catalyst support obtained by the preparation method described in any one of claims 6-12, and the platinum group metal active component loaded on the support material.

14. The catalyst according to claim 13, characterized in that, The platinum group metal active component is selected from one or more of ruthenium, rhodium, osmium, platinum and palladium.

15. The catalyst according to claim 14, characterized in that, The content of platinum group metal active components is 0.01-5.0% of the catalyst weight, calculated as elemental metal.

16. The catalyst according to claim 15, characterized in that, The content of platinum group metal active components is 0.05-1.0% of the catalyst weight, calculated as elemental metal.

17. The method for preparing the catalyst according to any one of claims 13-16, characterized in that, Includes the following steps: The catalyst support was impregnated in an aqueous solution containing platinum group metal element compounds, then removed and dried and calcined.

18. The use of the catalyst according to any one of claims 13-16 or the catalyst prepared according to the method of claim 17 in the dehydrogenation of saturated hydrocarbons to produce unsaturated hydrocarbons.

19. The application according to claim 18, characterized in that, The saturated hydrocarbon is ethylbenzene, and the unsaturated hydrocarbon is styrene.

20. A method for producing unsaturated hydrocarbons by dehydrogenation of saturated hydrocarbons, comprising subjecting hydrogen produced by the dehydrogenation of saturated hydrocarbons to a selective oxidation reaction in the presence of a catalyst according to any one of claims 13-16 or a catalyst prepared according to the method of claim 17.

21. The method according to claim 20, characterized in that, The conditions for the selective oxidation reaction include a reaction temperature of 520-650℃, a reaction pressure of 20-200 kPa, and a liquid hourly space velocity of 0.1-10 h⁻¹. -1 .

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