Preparation of platinum-ruthenium bimetallic catalyst and method for applying platinum-ruthenium bimetallic catalyst to hydrogenation of organic hydrogen carrier

Abstract

The invention belongs to the technical field of catalyst materials and hydrogen energy, and relates to a preparation method of a platinum-ruthenium bimetallic catalyst and an application method of the platinum-ruthenium bimetallic catalyst in hydrogenation of an organic hydrogen carrier. According to the technical scheme, the bimetallic catalyst contains a carrier and an active metal component, the carrier is porous alumina or other carriers, and the active metal component is a mixture of platinum and ruthenium components. The preparation method of the catalyst is an impregnation method, and comprises the following steps: preparing an alumina carrier, impregnating a metal precursor, roasting after impregnation, and carrying out reduction treatment. The invention also provides a process method for applying the catalyst to hydrogenation reaction of the organic hydrogen carrier. The process method comprises the following steps: adding the catalyst and the organic hydrogen carrier into a reaction container of a reaction kettle by adopting a kettle type reactor; the organic hydrogen carrier is benzyl toluene, dibenzyl toluene and the like. The preparation method of the platinum-ruthenium bimetallic catalyst, provided by the invention, has relatively high universality, is particularly suitable for the hydrogenation field of organic hydrogen carriers, and is beneficial to promoting the development of the technical field of hydrogen energy.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of catalyst materials and hydrogen energy technology, and particularly relates to a preparation method of a platinum-ruthenium bimetallic catalyst and an application method of the platinum-ruthenium bimetallic catalyst in hydrogenation of an organic hydrogen carrier. BACKGROUND

[0002] In the hydrogen energy related industrial chain, the current situation of "difficult storage and transportation" of hydrogen gas, which is determined by the characteristics of hydrogen gas itself, hinders the large-scale application of hydrogen energy. Existing hydrogen storage technologies include high-pressure gaseous hydrogen storage technology, low-temperature liquid hydrogen storage technology, solid hydrogen storage technology, and organic liquid hydrogen storage technology, etc. Organic liquid hydrogen storage technology stands out among the crowd of hydrogen storage technologies due to its high safety and high hydrogen storage capacity. This technology consists of two parts: hydrogen-poor organic hydrogen carrier hydrogenation and corresponding hydrogen-rich organic hydrogen carrier dehydrogenation after hydrogenation. As the first step of organic liquid hydrogen storage technology, researchers have carried out a series of studies on hydrogen-poor organic hydrogen carrier hydrogenation reactions. However, the current hydrogenation reactions of hydrogen-poor organic hydrogen carriers such as benzyltoluene generally have low hydrogenation catalyst activity, low hydrogenation catalyst selectivity, high hydrogenation pressure, and high hydrogenation temperature.

[0003] The literature (Int. J. Hydrogen Energy, 2024, 49, 1586-1596) reports the hydrogenation kinetics of benzyltoluene catalyzed by Ni / Al2O3 catalyst, and considers that the benzyltoluene hydrogenation reaction consists of the formation of intermediate product hexahydrobenzyltoluene from benzyltoluene hydrogenation and the formation of dodecahydrobenzyltoluene from hexahydrobenzyltoluene hydrogenation, where the hexahydrobenzyltoluene hydrogenation step is the rate-determining step.

[0004] The literature (Int. J. Hydrogen Energy, 2021, 286, 119889) compares the hydrogenation activity of Ru / MgO and Ru / Al2O3 catalysts applied in benzyltoluene hydrogenation reaction, and finds that the hydrogenation activity of Ru / MgO catalyst is significantly better than that of Ru / Al2O3.

[0005] The literature (J. Mater. Chem. A, 2024, 12, 23392-23397) discusses the microstructure sensitivity of platinum catalyst in toluene hydrogenation reaction, and finds that by controlling the electronic structure of platinum nanoparticles, the d-band center can be adjusted, thereby effectively regulating the adsorption of hydrogenation product methylcyclohexane on the surface of platinum nanoparticle catalyst and regulating the hydrogenation reaction of toluene.

[0006] Research on hydrogenation using organic hydrogen carriers, as exemplified by the aforementioned studies, reveals that current researchers primarily employ single-metal catalysts such as platinum, nickel, and ruthenium. However, these catalysts often suffer from low catalytic activity, low selectivity, and high loading of active components. Therefore, there is a need in this field for catalyst synthesis technologies and application processes that possess high hydrogenation activity for organic hydrogen carriers. Summary of the Invention

[0007] In response to the technical needs in this field, the present invention aims to prepare a highly active platinum-ruthenium bimetallic catalyst by proposing a widely applicable method for preparing the catalyst, and to apply the catalyst to the hydrogenation reaction of organic hydrogen carriers such as benzyltoluene and dibenzyltoluene.

[0008] The technical solution adopted in this invention is:

[0009] This invention provides a bimetallic catalyst comprising a support and an active metal component. The support is porous alumina, and the active metal component is a mixture of platinum and ruthenium components, wherein the mass ratio of platinum to ruthenium is 6:1 to 1:5. In the ruthenium component, ruthenium mainly exists in the form of zero-valent ruthenium; in the platinum component, platinum mainly exists in the form of zero-valent platinum. Titanium dioxide, hydrotalcite, molecular sieves, etc., can be used as the support. The mass ratio of the total metal component (the sum of the mass of platinum and ruthenium components) to the support is 1:5 to 1:300.

[0010] The mass ratio of platinum to ruthenium is 6:1 to 1:5, and can be 6:1, 5:1, 4:1, 3:1, 2:1, 1:1, 1:2, 1:3, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0011] The mass ratio of the total metal component (the sum of the mass of platinum and ruthenium metal components) to the carrier is 1:9 to 1:300, such as 1:9, 1:10, 1:11, 1:12, 1:13, 1:14, 1:15, 1:16, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0012] Furthermore, based on the target characteristic bimetallic catalyst, the present invention also provides a preparation method, which is an impregnation method, specifically comprising the following steps:

[0013] S1. Prepare an alumina carrier with the following characteristics: surface area of ​​180–400 m². 2The water absorption rate at room temperature is 0.6–1.2 g water / g. Alumina supports meeting the above physicochemical properties are dried in an oven and then calcined in a muffle furnace for 3–8 hours at 300–700°C in an air atmosphere. Titanium dioxide, hydrotalcite, molecular sieves, etc., can also be used as catalyst supports to replace the aforementioned alumina supports.

[0014] S2. Impregnation of the metal precursor, specifically as follows: Ruthenium acetate is used as the ruthenium component precursor, and chloroplatinic acid is used as the platinum component precursor. An aqueous solution is prepared, wherein the mass ratio of platinum to ruthenium in the aqueous solution is 6:1 to 1:5, and the mass ratio of the total mass of platinum and ruthenium components to water is 1:5 to 1:300. This metal precursor aqueous solution is mixed with the above-mentioned alumina support at a ratio of 0.9:1 to complete the impregnation of the alumina support with the precursor aqueous solution; the mixture of the precursor aqueous solution and the alumina support is left at room temperature for 4 to 12 hours.

[0015] S3. After impregnation, the product is calcined. The specific steps are as follows: the product obtained in S2 is dried in an oven at atmospheric pressure and 100-130°C for 1-8 hours. After drying, the product is transferred to a muffle furnace for calcination at 300-700°C for 3-8 hours.

[0016] S4. Reduction treatment, the specific procedure is as follows: Place the product obtained in step S3 in a tube furnace and reduce the product with hydrogen gas in the tube furnace. The reduction temperature is 300-700℃, the heating rate is 1-10℃ / min, and after reaching the target temperature, the holding time is 3-8h. Then, allow it to cool naturally while maintaining a hydrogen atmosphere during the cooling process. From the start of heating to cooling to near room temperature, maintain a hydrogen flow rate of 30-80ml / min in the furnace tube.

[0017] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the calcination time in step S1 is 3 to 8 hours, wherein the time can be 3 hours, 4 hours, 8 hours, etc., but is not limited to the listed values.

[0018] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the calcination temperature in step S1 is 300-700℃, wherein the temperature can be 300℃, 400℃, 500℃, 600℃, etc., but is not limited to the listed values.

[0019] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the mass ratio of platinum metal to ruthenium metal in the aqueous solution in step S2 is 6:1 to 1:5, wherein the mass ratio can be 6:1, 5:1, 4:1, 3:1, 1:3, 1:4, etc., but is not limited to the values ​​listed.

[0020] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the mass ratio of the total mass of platinum metal and ruthenium metal components to water in step S2 is 1:5 to 1:300. The mass ratio can be 1:5, 1:10, 1:100, 1:200, 1:300, etc., but is not limited to the values ​​listed.

[0021] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the drying temperature in step S3 is 100-130°C, wherein the temperature can be 100°C, 110°C, 120°C, 130°C, etc., but is not limited to the listed values.

[0022] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the drying time in step S3 is 1 to 8 hours, wherein the time can be 1 hour, 3 hours, 6 hours, 8 hours, etc., but is not limited to the listed values.

[0023] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the calcination is carried out in a muffle furnace in step S3 at a temperature of 300-700°C. The temperature can be 300°C, 400°C, 500°C, 600°C, 700°C, etc., but is not limited to the listed values.

[0024] As a method for preparing platinum-ruthenium bimetallic catalyst provided by the present invention, the calcination time in the muffle furnace in step S3 is 3 to 8 hours, wherein the time can be 3 hours, 4 hours, 6 hours, 8 hours, etc., but is not limited to the listed values.

[0025] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the reduction temperature in step S4 is 300-700℃, wherein the temperature can be 300℃, 400℃, 500℃, 600℃, etc., but is not limited to the listed values.

[0026] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the heating rate during the reduction process in step S4 is 1 to 10 °C / min, wherein the heating rate can be 2 °C / min, 4 °C / min, 6 °C / min, 8 °C / min, etc., but is not limited to the values ​​listed.

[0027] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the calcination temperature in step S4 is 300-700℃, wherein the temperature can be 400℃, 500℃, 600℃, etc., but is not limited to the listed values.

[0028] As a method for preparing platinum-ruthenium bimetallic catalyst provided by the present invention, the holding time during the hydrogen heat preservation process in step S4 is 3 to 8 hours, wherein the time can be 3 hours, 4 hours, 6 hours, 8 hours, etc., but is not limited to the listed values.

[0029] As a method for preparing a platinum-ruthenium bimetallic catalyst provided by the present invention, the hydrogen flow rate in step S4 is 30-80 ml / min, wherein the hydrogen flow rate can be 30 ml / min, 40 ml / min, 50 ml / min, 80 ml / min, etc., but is not limited to the values ​​listed.

[0030] Furthermore, based on the platinum-ruthenium bimetallic catalyst synthesized by the above method, this invention also provides a process method for using it in hydrogenation reactions on organic hydrogen carriers, the specific steps of which are as follows:

[0031] A batch reactor was used. A certain amount of the above-mentioned catalyst and a certain amount of organic hydrogen carrier were added to the reaction vessel of the reactor, with a mass ratio of 1:5 to 1:40. The organic hydrogen carrier was a potential organic hydrogen carrier such as benzyltoluene or dibenzyltoluene. Hydrogen gas was introduced into the reactor to replace the air in the reactor under closed conditions, and the replacement was performed 3 times. Then, a one-way valve was used to maintain the hydrogen pressure at 1 to 6 MPa. The hydrogen addition temperature in the reactor was controlled at 50 to 180°C, and the stirring rate was 100 to 1200 rpm. These conditions were maintained for 80 minutes, and then the reaction was stopped.

[0032] After cooling and depressurizing the reactor, the sample inside the reactor was taken out and subjected to solid-liquid separation; the product in the liquid phase was analyzed, and the degree of hydrogenation of the reaction was calculated.

[0033] The organic hydrogen carrier is a potential organic hydrogen carrier such as benzyltoluene or dibenzyltoluene. It can be toluene, benzyltoluene, dibenzyltoluene, biphenyl, etc., but is not limited to the listed organic hydrogen carriers. Other unlisted organic hydrogen carriers within this scope are also applicable.

[0034] The mass ratio of the platinum-ruthenium bimetallic catalyst to the benzyltoluene organic hydrogen carrier is 1:5 to 1:40. The mass ratio can be 1:5, 1:10, 1:15, 1:20, 1:30, 1:40, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0035] The hydrogen pressure is maintained between 1 and 6 MPa, where the pressure can be 2 MPa, 3 MPa, 4 MPa, 5 MPa, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0036] The hydrogenation temperature inside the reactor is 50–180°C. The temperature can be 50°C, 60°C, 70°C, 80°C, 90°C, 100°C, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0037] The stirring rate is 100 to 1200 rpm, and the stirring speed can be 200 rpm, 400 rpm, 600 rpm, 800 rpm, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0038] The innovative idea of ​​this invention is as follows: The provided bimetallic catalyst aims to regulate the dispersion of hydrogenation active sites in the bimetallic catalyst through the "synergistic effect" between the platinum metal component and the ruthenium metal component. At the same time, by means of electron transfer between the platinum metal component and the ruthenium metal component, the adsorption of benzyltoluene, hexahydrobenzyltoluene, and dodecahydrobenzyltoluene at the active sites is regulated, thereby promoting the hydrogenation reaction.

[0039] Using impregnation methods, especially under low heating rate process conditions, ensures the effectiveness of the catalyst.

[0040] The positive effects of this invention are as follows:

[0041] (1) This invention provides a method for achieving high hydrogenation of organic hydrogen carriers using a low platinum loading catalyst, thereby reducing catalyst usage costs. Currently, under reaction temperatures below 80°C, the degree of hydrogenation of benzyltoluene catalyzed by a 1.2 wt% platinum alumina catalyst within 80 min is often less than 30%, hindering the application of benzyltoluene in hydrogen storage. Using the catalyst and corresponding reaction process of this invention, the degree of hydrogenation can be increased to 86%.

[0042] (2) The preparation process of the platinum-ruthenium bimetallic catalyst provided by the present invention is simple and suitable for large-scale application.

[0043] (3) The preparation method of the platinum-ruthenium bimetallic catalyst provided by the present invention has great versatility and is especially suitable for the hydrogenation field of organic hydrogen carriers, which is conducive to promoting the development of hydrogen energy technology. Detailed Implementation

[0044] The technical solution of the present invention will be further illustrated below through specific embodiments.

[0045] Example 1

[0046] This invention provides a bimetallic catalyst comprising a support and an active metal component. The support is porous alumina, and the active metal component is a mixture of platinum and ruthenium components, wherein the mass ratio of platinum to ruthenium is 6:1 to 1:5. In the ruthenium component, ruthenium mainly exists in the form of zero-valent ruthenium; in the platinum component, platinum mainly exists in the form of zero-valent platinum; and the ratio of the total mass of platinum and ruthenium to the mass of alumina is 1:9 to 1:300.

[0047] In this example, the mass ratio of platinum to ruthenium is 3:4, and the ratio of the total mass of the two metal components to the mass of aluminum oxide is 1:34.5.

[0048] This embodiment also provides a method for preparing the above-mentioned bimetallic catalyst, which is an impregnation method, specifically including the following steps:

[0049] S1. Prepare an alumina carrier, which has the following characteristics: surface area of ​​184 m². 2 / g, with an average pore size of approximately 7.58nm and a water absorption rate of 0.9g water / g at room temperature; the alumina carrier that meets the above physicochemical properties is placed in an oven to dry and then transferred to a muffle furnace for calcination for 4 hours at a calcination temperature of 400℃ in an air calcination atmosphere;

[0050] S2. Impregnation of the metal precursor, specifically as follows: Ruthenium acetate is used as the ruthenium component precursor, and chloroplatinic acid is used as the platinum component precursor. An aqueous solution is prepared, wherein the mass ratio of platinum to ruthenium in the aqueous solution is 3:4, and the mass ratio of the total mass of platinum and ruthenium components to water is 1:31. This metal precursor aqueous solution is mixed with the above-mentioned alumina support at a ratio of 0.9:1 to complete the impregnation of the alumina support with the precursor aqueous solution; the mixture of the precursor aqueous solution and the alumina support is left at room temperature for 12 hours.

[0051] S3. After impregnation, the product is calcined. The specific steps are as follows: the product obtained in S2 is dried in an oven at atmospheric pressure and 100°C for 2 hours. After drying, the product is transferred to a muffle furnace for calcination at 450°C for 4 hours.

[0052] S4. Reduction treatment, the specific procedure is as follows: Place the product obtained in step S3 in a tube furnace and reduce the product in the tube furnace with hydrogen gas. The reduction temperature is 450℃, the heating rate is 5℃ / min, and after reaching the target temperature, the holding time is 4h. Then, allow it to cool naturally while maintaining a hydrogen atmosphere. From the start of heating to cooling to near room temperature, maintain a hydrogen flow rate of 45ml / min in the furnace tube.

[0053] Furthermore, this embodiment provides a process method for using the above-mentioned platinum-ruthenium bimetallic catalyst in the hydrogenation reaction of an organic hydrogen carrier, the specific steps of which are as follows:

[0054] A batch reactor was used. A certain amount of the above catalyst and a certain amount of organic hydrogen carrier were added to the reaction vessel of the reactor, with a mass ratio of 1:20. The organic hydrogen carrier was benzyltoluene. Under closed conditions, hydrogen gas was introduced to replace the air in the reactor, and the replacement was performed 3 times. Then, a one-way valve was used to maintain the hydrogen pressure at 4.5 MPa. The temperature in the reactor was controlled at 80℃, the stirring speed was 800 rpm, and the conditions were maintained for 80 min, after which the reaction was stopped.

[0055] After cooling and depressurizing the reactor, the sample inside the reactor was taken out and solid-liquid separation was performed; the product in the liquid phase was analyzed, and the degree of hydrogenation of the reaction was calculated to be 86%.

[0056] This invention focuses on developing bimetallic catalysts for the hydrogenation of organic hydrogen carriers (mainly benzyltoluene, but also including dibenzyltoluene, naphthalene, diphenylmethane, etc.), addressing the problem of low hydrogenation activity in current monometallic platinum-based catalysts. Currently, at temperatures ≤80℃, the degree of hydrogenation of benzyltoluene catalyzed by a 1.2 wt% platinum alumina catalyst is often below 30% within 80 min, hindering the application of benzyltoluene in hydrogen storage.

[0057] In this field, the physicochemical properties of catalysts, such as specific surface area and pore volume, are obtained through nitrogen adsorption-desorption experiments at 77K.

[0058] In this field, impregnation is a commonly used method for catalyst preparation. Its main steps involve dissolving the active metal component in water, where the volume of water is determined by the water absorption rate of the support, and the target concentration of the active metal component in the aqueous solution is determined by the target ratio of the metal to the support in the final catalyst product. To impregnate a larger amount of metal, a porous support with a large surface area is typically required. This method is common in the field, and its operational steps are well known to those skilled in the art.

[0059] In this embodiment, the mass ratio of the total mass of platinum and ruthenium metal components to water is 1:31, which is determined by the ratio of the total mass of the two components to the mass of alumina of 1:34.5, and the water absorption rate of alumina is 0.9g water / g.

[0060] In the above-mentioned catalyst preparation process, the main purpose of using ovens, muffle furnaces, and tube furnaces is to control the process conditions of catalyst preparation, not to limit the specific equipment used. In this field, the practice of using similar alternative methods to achieve the same process objective is a non-inventive extension and is in principle within the scope of protection of this case.

[0061] The above-mentioned liquid phase products were analyzed using elemental analyzers and gas chromatographs commonly used in this field, and the specific methods were conventional methods in this field; the formula for calculating the degree of hydrogenation (DoDH) obtained by product analysis using gas chromatography is as follows:

[0062]

[0063] DoDH=X 十二氢苄基甲苯 +0.5×X 六氢苄基甲苯 (1-3)

[0064] Where i represents benzyltoluene or hexahydrobenzyltoluene, dodecahydrobenzyltoluene; A i The peak area of ​​the chromatogram; m i M represents the mass fraction of a substance; i Molecular weight g·mol -1 ;X i Represents the mole fraction.

[0065] Example 2

[0066] Everything else is the same as in Example 1, except that:

[0067] The mass ratio of platinum to ruthenium is 3:1.

[0068] Example 3

[0069] Everything else is the same as in Example 1, except that:

[0070] The rotation speed in the hydrogenation reaction of benzyltoluene is 600 rpm.

[0071] Comparative Example 1

[0072] Everything else is the same as in Example 1, except that:

[0073] This comparative example does not involve impregnation of the ruthenium metal component; instead, the platinum metal component is impregnated onto alumina to obtain a single-metal platinum catalyst.

[0074] The catalyst reaction performance of the catalysts prepared in Examples 1-3 and Comparative Example 1 was evaluated, and the hydrogenation results are as follows:

[0075] The test results of the degree of hydrogenation of Examples 1-3 and Comparative Example 1 are shown in Table 1.

[0076] Table 1. Test results of hydrogenation degree in Examples 1-3 and Comparative Example 1

[0077] Degree of hydrogenation (%) Example 1 86.0 Example 2 33.8 Example 3 79.6 Comparative Example 1 Comparative Example 2 15.3

[0078] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A bimetallic catalyst, and a method for hydrogenation of an organic hydrogen carrier based on the bimetallic catalyst, characterized in that: The bimetallic catalyst contains a support and an active metal component, wherein the support is porous alumina and the active metal component is a mixture of platinum and ruthenium components, wherein the mass ratio of platinum to ruthenium metal is 6:1 to 1:

5. In the ruthenium metal component, ruthenium mainly exists in the form of zero-valent ruthenium; in the platinum metal component, platinum mainly exists in the form of zero-valent platinum; titanium dioxide, hydrotalcite, molecular sieves and other carriers can be selected, and the mass ratio of the total metal component (the sum of the mass of platinum metal component and ruthenium metal component) to the carrier is 1:5 to 1:

300. The mass ratio of the platinum to ruthenium metal is 6:1 to 1:5, and can be 6:1, 5:1, 4:1, 3:1, 2:1, 1:1, 1:2, 1:3, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable. The mass ratio of the total metal component (the sum of the mass of platinum and ruthenium metal components) to the carrier is 1:9 to 1:300, such as 1:9, 1:10, 1:11, 1:12, 1:13, 1:14, 1:15, 1:16, etc., but is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

2. The bimetallic catalyst according to claim 1, characterized in that, The bimetallic catalyst is prepared by impregnation, which specifically includes the following steps: S1. Prepare an alumina carrier with the following characteristics: surface area of ​​180–400 m². 2 The water absorption rate at room temperature is 0.6–1.2 g water / g. For alumina supports that meet the above physicochemical properties, they are placed in an oven to dry and then transferred to a muffle furnace for calcination for 3–8 hours at a temperature of 300–700°C in an air atmosphere. The catalyst support can also be titanium dioxide, hydrotalcite, molecular sieves, etc., to replace the above alumina supports. S2. Impregnation of metal precursors, the specific procedure is as follows: Ruthenium acetate is used as the ruthenium component precursor, and chloroplatinic acid is used as the platinum component precursor. An aqueous solution is prepared, wherein the mass ratio of platinum metal to ruthenium metal components in the aqueous solution is 6:1 to 1:5, and the mass ratio of the total mass of platinum metal to ruthenium metal components to water is 1:5 to 1:300; the aqueous solution of the metal precursor is mixed with the above-mentioned alumina support at a ratio of 0.9:1 to complete the impregnation of the alumina support with the precursor aqueous solution; the mixture of the above-mentioned precursor aqueous solution and alumina support is placed at room temperature for 4 to 12 hours; S3. After impregnation, the product is calcined. The specific steps are as follows: the product obtained in S2 is dried in an oven at atmospheric pressure and 100-130°C for 1-8 hours. After drying, the product is transferred to a muffle furnace for calcination at 300-700°C for 3-8 hours. S4. Reduction treatment, the specific procedure is as follows: Place the product obtained in step S3 in a tube furnace and reduce the product with hydrogen gas in the tube furnace. The reduction temperature is 300-700℃, the heating rate is 1-10℃ / min, and after reaching the target temperature, the holding time is 3-8h. Then, allow it to cool naturally while maintaining a hydrogen atmosphere during the cooling process. From the start of heating to cooling to near room temperature, maintain a hydrogen flow rate of 30-80ml / min in the furnace tube.

3. The bimetallic catalyst according to claim 1, the method for hydrogenation of organic hydrogen carriers based on the bimetallic catalyst, and the catalyst preparation method according to claim 2, characterized in that: The specific process for using the platinum-ruthenium bimetallic catalyst synthesized by the above method in the hydrogenation reaction of organic hydrogen carriers is as follows: A batch reactor was used. A certain amount of the above-mentioned catalyst and a certain amount of organic hydrogen carrier were added to the reaction vessel of the reactor, with a mass ratio of 1:5 to 1:

40. The organic hydrogen carrier was a potential organic hydrogen carrier such as benzyltoluene or dibenzyltoluene. Hydrogen gas was introduced into the reactor to replace the air in the reactor under closed conditions, and the replacement was performed 3 times. Then, a one-way valve was used to maintain the hydrogen pressure at 1 to 6 MPa. The hydrogen addition temperature in the reactor was controlled at 50 to 180°C, and the stirring rate was 100 to 1200 rpm. These conditions were maintained for 80 minutes, and then the reaction was stopped. After cooling and depressurizing the reactor, the sample inside the reactor was removed and subjected to solid-liquid separation; the product in the liquid phase was analyzed, and the degree of hydrogenation of the reaction was calculated. The organic hydrogen carrier is a potential organic hydrogen carrier such as benzyltoluene or dibenzyltoluene. It can be toluene, benzyltoluene, dibenzyltoluene, biphenyl, etc., but is not limited to the listed organic hydrogen carriers. Other unlisted organic hydrogen carriers within this scope are also applicable.

4. The bimetallic catalyst according to claim 1, and the method for hydrogenation of organic hydrogen carriers based on the bimetallic catalyst, characterized in that: The degree of hydrogenation of the organic hydrogen carrier is not less than 30%.

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