Dehydrogenation catalyst, method for preparing and using the same, and alkane dehydrogenation method

Abstract

The present application relates to the technical field of dehydrogenation, in particular to a dehydrogenation catalyst, a preparation method and application thereof, and an alkane dehydrogenation method. The catalyst contains a carrier, chromium oxide, an auxiliary agent and a solid solution promoter supported on the carrier, the solid solution promoter is selected from one or more of gallium oxide, magnesium oxide and vanadium oxide; wherein the ratio of the central chromium content to the edge chromium content of the catalyst is 0.7-1.1. The catalyst of the present application is used for dehydrogenation reactions such as alkane dehydrogenation reactions, which can effectively reduce the occurrence of side reactions while ensuring high selectivity of the product, and improve the yield of by-product hydrogen.

Description

Technical Field

[0001] This invention relates to the field of dehydrogenation technology, specifically to a dehydrogenation catalyst, its preparation method and application, and a method for dehydrogenating alkane. Background Technology

[0002] Propylene is a crucial raw material for the production of chemical products such as polypropylene and propylene oxide. Currently, propylene production processes mainly include naphtha cracking and catalytic cracking via the petroleum route, coal-to-olefins via the coal chemical route, and propane dehydrogenation via the natural gas route. Under the dual-carbon development goals, propane dehydrogenation is rapidly developing in China, with enormous market potential. Developing suitable propane dehydrogenation catalysts has significant economic value. Among these, chromium-based catalysts, with their advantages of low cost and high activity, have become a research hotspot.

[0003] Current research on chromium-based propane dehydrogenation catalysts mainly focuses on improving propylene selectivity and stability. CN105727930B discloses a propane dehydrogenation catalyst for propylene production, employing an alumina-zirconia or alumina-cerium oxide composite oxide support, achieving high conversion and propylene selectivity. CN107715862B discloses a chromium-based propane dehydrogenation catalyst resistant to carbon deposition, using rod-shaped alumina rich in unsaturated coordination as a support to prevent chromium oxide agglomeration, thus maintaining high propylene selectivity and improving stability. CN110152650B discloses a supported catalyst for propane dehydrogenation, which significantly improves catalyst stability and lifespan by employing a high-temperature sintering-resistant, phase-transformation-resistant support with a high specific surface area at high temperatures.

[0004] However, the utilization of by-product hydrogen in propane dehydrogenation has not received sufficient attention and still needs further improvement. By-product hydrogen from propane dehydrogenation is mostly consumed by specific side reactions in the process, such as the hydrogenation of ethylene, a cracking product. If the product distribution of the propane dehydrogenation reaction can be optimized, while maintaining high propylene selectivity and stability, reducing ethane selectivity and increasing hydrogen yield, it will not only improve the economics of the propane dehydrogenation process but also provide inexpensive, low-carbon-emission hydrogen resources, which is beneficial for hydrogen energy development and further expands the applicability of the propane dehydrogenation process. Summary of the Invention

[0005] The purpose of this invention is to overcome the problem in the existing dehydrogenation process where hydrogen participates in side reactions, leading to hydrogen consumption. This invention provides a dehydrogenation catalyst, its preparation method, its application, and an alkane dehydrogenation method. The chromium content in the catalyst's center is similar to that in the catalyst's edge. When used in hydrocarbon dehydrogenation reactions, this catalyst effectively reduces the occurrence of side reactions and increases the yield of byproduct hydrogen while ensuring high product selectivity.

[0006] To achieve the above objectives, a first aspect of the present invention provides a dehydrogenation catalyst comprising a support and chromium oxide, an auxiliary agent, and a solid solution promoter supported on the support, wherein the solid solution promoter is selected from one or more of gallium oxide, magnesium oxide, and vanadium oxide; wherein the ratio of the central chromium content to the peripheral chromium content of the catalyst is 0.7-1.1.

[0007] A second aspect of the present invention provides a method for preparing the catalyst of the present invention, the method comprising: loading a chromium source, an auxiliary source and a solid solution promoter source onto a support to obtain a catalyst precursor, and calcining the catalyst precursor to obtain the catalyst.

[0008] A third aspect of the present invention provides the application of the catalyst described herein in hydrocarbon dehydrogenation reactions.

[0009] A fourth aspect of the present invention provides a method for dehydrogenating alkanes, the method comprising: dehydrogenating alkanes in the presence of hydrogen sulfide in the presence of the catalyst described in the present invention.

[0010] The dehydrogenation catalyst provided by this invention contains a support and chromium oxide, an additive, and a solid solution promoter supported on the support. The solid solution promoter is selected from one or more of gallium oxide, magnesium oxide, and vanadium oxide. The ratio of central chromium to peripheral chromium in the catalyst is 0.7-1.1. Compared with the prior art, in the catalyst of this invention, the chromium element distributed in the center of the catalyst is similar to that distributed in the edge of the catalyst. When this catalyst is used for dehydrogenation reactions such as alkane dehydrogenation reactions (e.g., propane dehydrogenation), while ensuring high selectivity of the product (propylene), it can effectively reduce the occurrence of side reactions (e.g., by-product ethane reaction) and increase the yield of by-product hydrogen.

[0011] In a preferred embodiment of the present invention, the dehydrogenation catalyst preparation process, by adding a solid solution promoter and other steps and conditions, can prepare a dehydrogenation catalyst with excellent performance. As a further preferred embodiment, in the process of preparing a solution containing a chromium source, an auxiliary source and a solid solution promoter source, the catalyst prepared by adding an organic acid to adjust the pH can be used for dehydrogenation, such as alkane dehydrogenation reaction, which can further reduce the occurrence of side reactions (such as by-product ethane reaction) and can further increase the yield of by-product hydrogen. Detailed Implementation

[0012] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0013] In this invention, the method for detecting the ratio of central chromium to edge chromium in a catalyst is as follows: the catalyst is worn down to 50% of its total mass to obtain remaining catalyst particles and powder. The chromium content in the remaining catalyst particles is the central chromium content, and the chromium content in the powder is the edge chromium content.

[0014] In this invention, the chromium content is obtained through ICP analysis.

[0015] In this invention, the catalyst can be worn down using a wear tester until the worn-down mass of the catalyst is 50% of the total mass.

[0016] The first aspect of the present invention provides a dehydrogenation catalyst comprising a support and chromium oxide, an auxiliary agent and a solid solution promoter supported on the support, wherein the solid solution promoter is selected from one or more of gallium oxide, magnesium oxide and vanadium oxide; wherein the ratio of the central chromium content to the peripheral chromium content of the catalyst is 0.7-1.1.

[0017] In this invention, the elemental content of the catalyst is determined by ICP analysis.

[0018] According to a preferred embodiment of the present invention, the ratio of the central chromium content to the peripheral chromium content of the catalyst is 0.8-1.02.

[0019] According to a preferred embodiment of the present invention, the catalyst has a specific surface area of ​​93-120 m². 2 / g, with a pore volume of 0.25-0.40ml / g.

[0020] In this invention, the catalyst contains a wide range of selectable contents, including the active metal chromium, the auxiliary agent, and the solid solution promoter. According to a preferred embodiment of the invention, based on the total amount of catalyst and in terms of elemental content, the chromium content is 5-20% by weight, the auxiliary agent content is 0.1-5% by weight, and the solid solution promoter content is 0.1-2% by weight; preferably, the chromium content is 8-15% by weight, the auxiliary agent content is 0.5-2.5% by weight, and the solid solution promoter content is 0.5-1% by weight. Using the aforementioned preferred scheme can further reduce the dehydrogenation byproducts in the dehydrogenation process.

[0021] In this invention, there are no special requirements for the auxiliary elements. Commonly used auxiliary elements can be used in this invention. For this invention, it is preferred that the auxiliary elements are selected from one or more of Group IA metals, Group IVB metals and Group VIII metals, and preferably at least one of sodium, potassium, zirconium and cobalt.

[0022] According to a preferred embodiment of the present invention, the adjuvant is sodium and / or potassium.

[0023] In this invention, the solid solution promoter is selected from at least two of gallium oxide, magnesium oxide, and vanadium oxide. According to a preferred embodiment of the invention, the solid solution promoter is preferably a mixture of gallium oxide and magnesium oxide, and more preferably, the mass ratio of gallium oxide to magnesium oxide is 1:0.2-0.3. This can further reduce the dehydrogenation byproducts in the dehydrogenation process.

[0024] In this invention, there are no special requirements for the carrier. Commonly used carriers can be used in this invention. For this invention, preferably, the carrier is selected from one or more of alumina, silicon dioxide, titanium dioxide and molecular sieves. More preferably, the carrier is selected from alumina of any crystal form, and more preferably, γ-alumina.

[0025] In this invention, the objective of the invention can be achieved as long as the catalyst possesses the characteristics described in this invention. There are no special requirements for the preparation method of the catalyst. Preferably, the second aspect of this invention provides a method for preparing the catalyst described in this invention, which includes: loading a chromium source, an auxiliary source and a solid solution promoter source onto a support to obtain a catalyst precursor, and calcining the catalyst precursor to obtain the catalyst.

[0026] According to a preferred embodiment of the present invention, the catalyst preparation comprises:

[0027] (1) Dissolve the chromium source, the auxiliary agent source and the solid solution accelerator source in a solvent to obtain a solution;

[0028] (2) The solution is mixed with the support and dried to obtain the catalyst precursor;

[0029] (3) The catalyst precursor is calcined to obtain the catalyst. By using the aforementioned preferred preparation method, the dehydrogenation byproducts in the dehydrogenation process can be further reduced.

[0030] In this invention, there are no special requirements for the dissolution conditions. According to a preferred embodiment of the invention, the dissolution conditions include a temperature of 40-90°C, preferably 50-80°C.

[0031] According to a preferred embodiment of the present invention, step (1) includes:

[0032] i) Mix the chromium source, the auxiliary agent source, and deionized water;

[0033] ii) The solution temperature is maintained at 40-90℃ by heating;

[0034] iii) Add the solid solution promoter source to the product obtained in step ii) to obtain a solution containing a chromium source, an auxiliary source, and a solid solution promoter source. Using the aforementioned preferred embodiment, the hydrocarbon dehydrogenation selectivity of the catalyst can be further improved, the occurrence of side reactions can be reduced, and the content of by-product hydrogen can be increased.

[0035] According to a preferred embodiment of the present invention, the mixing conditions in step i) are not particularly required, and can be static or dynamic mixing. The mixing time is determined as needed. According to a preferred embodiment of the present invention, the mixing conditions in step i) include: the mixing method is selected from mechanical stirring and ultrasonic stirring; the mixing time is 10-60 min.

[0036] According to a preferred embodiment of the present invention, the heating temperature in step ii) is 50-80°C. By employing the aforementioned preferred embodiment, the hydrocarbon dehydrogenation selectivity of the catalyst can be further improved, thereby reducing the occurrence of side reactions and increasing the content of by-product hydrogen.

[0037] According to a preferred embodiment of the present invention, in step i), an organic acid is added to adjust the pH to below 3.5. Preferably, the organic solvent is selected from one or more of citric acid, lactic acid, oxalic acid, and oxalic acid. By employing the aforementioned preferred embodiment, the hydrocarbon dehydrogenation selectivity of the catalyst can be further improved, thereby reducing the occurrence of side reactions and increasing the content of by-product hydrogen.

[0038] In this invention, there are no special requirements for the drying conditions, which are determined according to specific needs. According to a preferred embodiment of the present invention, the drying conditions include: a temperature of 60-180℃ and a time of 1-96h; preferably, a temperature of 120-150℃ and a time of 24-72h.

[0039] In this invention, there are no special requirements for the roasting conditions, which are determined according to specific needs. According to a preferred embodiment of this invention, the roasting conditions include: a roasting temperature of 500-850℃ and a roasting time of 6-24h.

[0040] In this invention, calcination can be carried out in various environments, such as an inert atmosphere or an oxygen-containing atmosphere. For this invention, it is preferred to carry out the calcination in an oxygen-containing atmosphere, such as an air atmosphere.

[0041] In this invention, there are no special requirements for the type of chromium source. Commonly used chromium sources can be used in this invention. For this invention, preferably, the chromium source is selected from one or more of soluble chromium compounds such as chromium salts and chromium anhydrides; preferably, the soluble chromium salt is selected from one or more of chromium nitrate, chromium acetate and chromium citrate, and more preferably, the chromium source is chromium anhydride.

[0042] In this invention, there are no special requirements for the type of auxiliary agent source; commonly used auxiliary agent sources can be used in this invention. Preferably, the auxiliary agent source is selected from one or more soluble salts of Group IA metal elements, Group IVB metal elements, and Group VIII metal elements; more preferably, it is a soluble salt of Group IA metal elements.

[0043] In this invention, there are no special requirements for the type of solid solution promoter source. Commonly used solid solution promoter sources can be used in this invention. Preferably, the solid solution promoter source is selected from one or more soluble compounds of gallium, magnesium and vanadium, such as salts.

[0044] A third aspect of this invention provides the application of the catalyst described herein in hydrocarbon dehydrogenation reactions. The catalyst of this invention, when used in hydrocarbon dehydrogenation reactions (e.g., propane dehydrogenation), effectively reduces the formation of byproducts (e.g., ethane) while ensuring high selectivity for products (e.g., propylene) and increasing the yield of byproduct hydrogen.

[0045] A fourth aspect of the present invention provides a method for dehydrogenating alkane, the method comprising:

[0046] In the presence of the catalyst described in this invention, alkanes are dehydrogenated.

[0047] This invention does not impose special requirements on the dehydrogenation conditions. According to a preferred embodiment of this invention, the dehydrogenation conditions preferably include: a temperature of 500-650°C, a pressure of 0.05-0.15 MPa, and a mass hourly space velocity (HSV) of 0.5-5 h⁻¹. -1 .

[0048] The catalyst of the present invention is suitable for various alkane dehydrogenation reactions and has no special requirements on the type of alkane. Preferably, the alkane is a C6 or smaller alkane, preferably a C1-C5 straight-chain or branched alkane, such as one or more of isobutane, n-butane and propane, and more preferably propane.

[0049] The present invention will be described in detail below through embodiments.

[0050] In the following examples, the gas composition before and after the reaction was determined by online gas chromatography. Specifically, it was measured using an Agilent GC7890 gas chromatograph. The formulas for calculating the conversion and selectivity are as follows:

[0051]

[0052]

[0053] In the following examples, the content of each element was determined by inductively coupled plasma atomic emission spectrometry (ICP). Specifically, it was measured using a THERMO IRIS Intrepid XSP inductively coupled plasma atomic emission spectrometer.

[0054] In the following examples, the specific surface area and pore volume of the catalyst were tested using a BET adsorption-desorption apparatus.

[0055] Example 1

[0056] (1) Dissolve 3.7926g of chromium trioxide and 0.2429g of sodium nitrate in 10g of deionized water, heat to 80℃, sonicate for 60min, add 0.7876g of gallium nitrate nonahydrate, sonicate for 60min to obtain a solution;

[0057] (2) Mix 10g of γ-alumina with the solution in step (1) and dry at 120℃ for 24h to obtain the catalyst precursor;

[0058] (3) The catalyst precursor was calcined at 800°C for 6 hours in air atmosphere to obtain the catalyst, denoted as A1.

[0059] Catalyst evaluation:

[0060] At a temperature of 600℃, a pressure of 0.1MPa, and a mass hourly space velocity of 1h... -1 Under the given conditions, the obtained catalyst A1 was reacted with propane for 4 hours to obtain propane conversion and ethane selectivity data.

[0061] The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity and propylene selectivity are shown in Table 2.

[0062] Example 2

[0063] (1) Dissolve 1.1828 g of chromium trioxide and 0.8963 g of zirconium nitrate trihydrate in 10 g of deionized water, heat to 40 °C, sonicate for 60 min, add 0.2079 g of magnesium nitrate, and sonicate for 60 min to obtain a solution;

[0064] (2) Mix 10g of γ-alumina with the solution in step (1) and dry at 120℃ for 72h to obtain the catalyst precursor;

[0065] (3) The catalyst precursor was calcined at 500°C for 24 hours in air atmosphere to obtain the catalyst, denoted as A2.

[0066] Catalyst evaluation:

[0067] At a temperature of 600℃, a pressure of 0.1MPa, and a mass hourly space velocity of 1h... -1 Under the given conditions, the obtained catalyst A2 was reacted with propane for 4 hours to obtain propane conversion and ethane selectivity data.

[0068] The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity and propylene selectivity are shown in Table 2.

[0069] Example 3

[0070] (1) Dissolve 14.4192 g of chromium nitrate nonahydrate and 0.8963 g of potassium nitrate in 10 g of deionized water, heat to 50 °C, stir mechanically for 60 min, add 0.3524 g of ammonium metavanadate, stir mechanically for 60 min, and obtain a solution;

[0071] (2) Mix 10g of γ-alumina with the solution in step (1) and dry at 60℃ for 96h to obtain the catalyst precursor;

[0072] (3) The catalyst precursor was calcined at 500°C for 24 hours in air atmosphere to obtain the catalyst, denoted as A3.

[0073] Catalyst evaluation:

[0074] At a temperature of 600℃, a pressure of 0.1MPa, and a mass hourly space velocity of 1h... -1 Under the given conditions, the obtained catalyst A3 was reacted with propane for 4 hours to obtain propane conversion and ethane selectivity data.

[0075] The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity and propylene selectivity are shown in Table 2.

[0076] Example 4

[0077] Following the method of Example 1, except that the amount of chromic anhydride was 2.3384 g, the amount of sodium nitrate was 0.1623 g, and the amount of gallium nitrate nonahydrate was 0.0526 g, while the other conditions were the same as in Example 1; catalyst A4 was obtained. The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity, and propylene selectivity are shown in Table 2.

[0078] Example 5

[0079] Following the method of Example 1, except that gallium nitrate nonahydrate was replaced with gallium nitrate nonahydrate and magnesium nitrate, with the amount of gallium nitrate nonahydrate being 0.3704 g and the amount of magnesium nitrate being 0.0614 g, and the other conditions being the same as in Example 1; catalyst A5 was obtained. The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity, and propylene selectivity are shown in Table 2.

[0080] Example 6

[0081] The method of Example 1 is different except that step (1) is performed as follows:

[0082] Dissolve 3.7926 g of chromic anhydride, 0.2429 g of sodium nitrate, and 0.7876 g of gallium nitrate nonahydrate in 10 g of deionized water, heat to 80 °C, and sonicate for 120 min to obtain a solution; all other conditions are the same.

[0083] Catalyst A6 was obtained, and the catalyst test results are shown in Table 1. Propane conversion, ethane selectivity and propylene selectivity are shown in Table 2.

[0084] Example 7

[0085] The method is the same as in Example 1, except that citric acid is added in step (1), as follows:

[0086] 3.7926 g of chromic anhydride and 0.2429 g of sodium nitrate were dissolved in 10 g of deionized water. Citric acid was added to adjust the pH to 3.5, and the solution was heated to 80 °C and ultrasonically stirred for 60 min. Then, 0.7876 g of gallium nitrate nonahydrate was added and ultrasonically stirred for 60 min to obtain the solution. The remaining conditions were the same as in Example 1. Catalyst A7 was obtained. The catalyst test results are shown in Table 1, and the propane conversion, ethane selectivity, and propylene selectivity are shown in Table 2.

[0087] Comparative Example 1

[0088] (1) Dissolve 3.7267 g of chromium anhydride and 0.2388 g of sodium nitrate in 10 g of deionized water, heat to 80 °C, and sonicate for 60 min to obtain a solution;

[0089] (2) Mix 10g of γ-alumina with the solution and dry at 120℃ for 24h to obtain the catalyst precursor;

[0090] (3) Catalyst: The precursor was calcined at 800°C for 6 hours in air atmosphere to obtain the catalyst, denoted as D1.

[0091] The catalyst evaluation conditions are the same as in Example 1.

[0092] The chromium content, central chromium to edge chromium ratio, metal oxide additive content, and solid solution promoter content of catalyst D1 are shown in Table 1. The propane conversion rate, ethane selectivity, and propylene selectivity are shown in Table 2.

[0093] Table 1

[0094]

[0095]

[0096] Table 2

[0097] Example 1 0.7 91.5 54.3 Example 2 0.83 92.2 51.6 Example 3 1.89 90.8 54.1 Example 4 1.70 91.3 49.2 Example 5 0.57 91.7 54.1 Example 6 0.98 90.4 50.1 Example 7 0.53 92.5 54.5 Comparative Example 1 4.3 91.8 53.6

[0098] As can be seen from the results in Table 2, compared with Comparative Example 1, the catalyst of the present invention has a central chromium to edge chromium ratio in the range of 0.7-1.1. While achieving high selectivity for propylene, it can effectively reduce the occurrence of side reactions (byproduct ethane reaction) and increase the yield of byproduct hydrogen.

[0099] In the catalyst preparation process, Example 7 of this invention, which introduces organic acids and solid solution promoters, exhibits the lowest ethane selectivity, the highest propane conversion rate, and the highest propylene selectivity. It can also further increase the yield of by-product hydrogen, resulting in significantly better performance.

[0100] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A dehydrogenation catalyst, characterized in that, The catalyst contains a support and chromium oxide, an additive, and a solid solution promoter supported on the support. The solid solution promoter is selected from gallium oxide and / or magnesium oxide. The additive element is selected from one or more of Group IA, Group IVB, and Group VIII metals. The ratio of the central chromium content to the peripheral chromium content of the catalyst is 0.8-1.

1.

2. The catalyst according to claim 1, wherein, The ratio of the central chromium content to the peripheral chromium content of the catalyst is 0.8-1.02; and / or The catalyst has a specific surface area of ​​93-120 m². 2 / g, and / or pore volume of 0.25-0.40ml / g.

3. The catalyst according to claim 1 or 2, wherein, Based on the total amount of catalyst, the chromium content is 5-20% by weight, the auxiliary agent content is 0.1-5% by weight, and the solid solution promoter content is 0.1-2% by weight.

4. The catalyst according to claim 1 or 2, wherein, Based on the total amount of catalyst, the chromium content is 8-15% by weight, the auxiliary agent content is 0.5-2.5% by weight, and the solid solution promoter content is 0.5-1% by weight.

5. The catalyst according to claim 1 or 2, wherein, The auxiliary element is selected from at least one of sodium, potassium, zirconium, and cobalt; The solid solution promoter is selected from a mixture of gallium oxide and magnesium oxide, wherein the mass ratio of gallium oxide to magnesium oxide is 1:0.2-0.3; and / or The carrier is selected from one or more of alumina, silica, molecular sieve and titanium dioxide.

6. The catalyst according to claim 1 or 2, wherein, The carrier is aluminum oxide.

7. The catalyst according to claim 1 or 2, wherein, The carrier is γ-alumina.

8. A method for preparing the catalyst according to any one of claims 1-7, characterized in that, The method includes: (1) Dissolve the chromium source, auxiliary agent source and solid solution accelerator source in a solvent to obtain a solution; (2) The solution is mixed with the support and dried to obtain the catalyst precursor; (3) The catalyst is obtained by calcining the catalyst precursor; Step (1) includes: i) Mix the chromium source, the auxiliary agent source, and deionized water; ii) The solution temperature is maintained at 50-80℃ by heating; iii) Add the solid solution promoter source to the product obtained in step ii) to obtain a solution containing a chromium source, an auxiliary source and a solid solution promoter source.

9. The preparation method according to claim 8, wherein, In step i), add an organic acid to adjust the pH to below 3.

5.

10. The preparation method according to claim 9, wherein, The organic acid is selected from one or more of citric acid, lactic acid, oxalic acid, and oxalic acid.

11. The preparation method according to claim 8 or 9, wherein, The drying conditions in step (2) include: a temperature of 60-180℃ and a time of 1-96 hours; and / or The roasting conditions in step (3) include: roasting temperature of 500-850℃ and roasting time of 6-24h.

12. The preparation method according to claim 11, wherein, The drying conditions in step (2) include: a temperature of 120-150℃ and a time of 24-72h.

13. The use of the catalyst according to any one of claims 1-7 in hydrocarbon dehydrogenation reactions.

14. A method for dehydrogenating alkane, characterized in that, The method includes: In the presence of the catalyst described in any one of claims 1-7, alkanes are dehydrogenated.

15. The alkane dehydrogenation method according to claim 14, wherein, The conditions for dehydrogenation include: a temperature of 500-650℃, a pressure of 0.05-0.15 MPa, and a mass hourly space velocity of 0.5-5 h⁻¹. -1 ; The alkane is an alkane with fewer than 6 carbon atoms.

16. The alkane dehydrogenation method according to claim 14, wherein the alkane is propane.

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