Single-atom catalyst for dehydrogenation of liquid organic hydrogen carrier, and preparation method therefor and use thereof

Abstract

To provide a single-atom catalyst for dehydrogenation of a liquid organic hydrogen carrier, and a preparation method therefor and the use thereof, in the field of catalysts.SOLUTION: The single-atom catalyst comprises a metal oxide carrier and precious-metal single atoms loaded on the oxide carrier. The obtained single-atom catalyst is applied to the process of a dehydrogenation reaction of a liquid organic hydrogen carrier; compared with metal particles, the single-atom catalyst exhibits better catalytic activity; moreover, the amount of precious metals used is effectively reduced, thereby reducing the cost of the catalyst.SELECTED DRAWING: None

Description

[Technical Field]

[0001] The present invention relates to the field of catalysis and to a single atom catalyst used in the dehydrogenation of liquid organic hydrogen storage carriers, its preparation method and use. [Background technology]

[0002] Hydrogen energy, as a renewable energy source with broad prospects, has been attracting increasing attention as a means of addressing the energy crisis. However, the problem of safe hydrogen storage and transportation significantly restricts the development of hydrogen energy. Liquid organic hydrogen carriers (LOHCs) can effectively solve these problems and are considered one of the key technologies expected to achieve carbon neutrality within a few decades.

[0003] LOHC is a method for storing and transporting hydrogen gas. It utilizes the reversible reaction between unsaturated liquid organic compounds, such as alkenes, alkynes, or aromatic hydrocarbons, and hydrogen gas to achieve hydrogen storage (chemical bonding) and release. The principle of this technology is to store hydrogen through a hydrogenation reaction and release hydrogen through a dehydrogenation reaction. Its features include a large hydrogen storage capacity, the ability to transport at room temperature and pressure, and convenience and safety.

[0004] Specifically, in LOHCs, hydrogen chemical bonds can be attached to organic hydrocarbon carrier molecules (hydrogenation) and released in the reverse process (dehydrogenation). Common LOHC systems, such as methylcyclohexane (MCH), dibenzyltoluene (DBT), or decahydronaphthalene / naphthol, typically exist as liquids at fairly moderate conditions and, in both their hydrogenated and dehydrogenated forms, have physical properties similar to those of conventional fossil fuels (e.g., diesel).

[0005] Therefore, LOHCs have many advantages. First, they overcome the challenges of hydrogen gas transportation and can be transported and stored in a more efficient, effective, and safer manner using existing infrastructure. Compared to liquid hydrogen, LOHCs are less flammable and therefore less expensive to transport, while liquid hydrogen is prone to explosion and evaporation, and requires expensive containers and new, dedicated infrastructure. Second, LOHCs are highly pure and non-toxic, ensuring purity with at least comparable reconversion costs, unlike ammonia, which poses safety and environmental issues. Furthermore, due to their physical similarity to conventional liquid fuels, LOHCs have the potential to be easy to use and transport within existing infrastructure.

[0006] This shows that while LOHCs have the potential to be used to meet global hydrogen supply and demand, their actual application and development will be limited by the development of catalysts suitable for larger-scale production and application. Catalysts play an important role in the hydrogenation and dehydrogenation processes, not only lowering the reaction temperature but also improving the reaction rate of chemical hydrogen storage technology. In recent years, research into dehydrogenation catalysts for liquid organic hydrogen carriers has focused on precious metal catalysts. However, these technologies have problems such as high precious metal loadings, uneven distribution of active components on the carrier, and a tendency for aggregation during the reaction process, resulting in low reaction activity.

[0007] Therefore, it is necessary to develop novel forms to solve the problems of conventional dehydrogenation catalysts, which has important practical significance for the large-scale application and development of LOHC. Summary of the Invention [Problem to be solved by the invention]

[0008] In view of the problems in the prior art, the present invention provides a single-atom catalyst for the dehydrogenation of liquid organic hydrogen carriers, as well as a method for preparing and using the same. The single-atom catalyst comprises a metal oxide support and a single-atom noble metal supported on the oxide support. When used in the dehydrogenation reaction of liquid organic hydrogen carriers, the single-atom catalyst exhibits superior catalytic activity compared with metal particles, and can effectively reduce the amount of noble metal used, thereby reducing catalyst costs. [Means for solving the problem]

[0009] To achieve this objective, the present invention provides the following technical solutions.

[0010] In aspect 1, the present invention provides a method for producing a pharmaceutical composition comprising: A catalyst comprising a metal oxide support and a noble metal monatom supported on the oxide support. A single atom catalyst for use in the dehydrogenation of liquid organic hydrogen carriers is provided.

[0011] The present invention constructs and applies the single-atom catalyst to the dehydrogenation reaction process of liquid organic hydrogen carriers. Compared with metal particles, the single-atom catalyst exhibits superior catalytic activity, effectively reduces the amount of precious metal used, and reduces catalyst costs.

[0012] The following is a preferred technical solution of the present invention, but is not intended to limit the technical solution of the present invention. The technical objectives and beneficial effects of the present invention can be better achieved and realized by the following technical solution.

[0013] In a preferred technical solution of the present invention, the metal oxide support comprises a transition metal oxide and / or a rare earth metal oxide.

[0014] Preferably, the metal oxide support contains any one of cerium oxide, titanium oxide, and zirconium oxide, and more preferably contains cerium oxide.

[0015] The oxygen vacancies in the specific metal oxide supports of the present invention make it easier to achieve monoatomic loading, whereas the inert support Al2O3, which lacks monoatomic anchoring sites, cannot achieve monoatomic loading through simple calcination.

[0016] Preferably, the noble metal includes at least one of Pt, Pd, and Rh. For example, typical combinations include, but are not limited to, a combination of Pt and Pd, a combination of Pt and Rh, or a combination of Pd and Rh.

[0017] Preferably, the amount of the noble metal monoatom supported is 0.1% to 5% when the mass of the metal oxide support is 100%, for example, 0.1%, 0.5%, 0.8%, 1%, 1.2%, 1.4%, 1.6%, 1.8%, 2%, 2.2%, 2.4%, 2.6%, 2.8%, 3%, 3.2%, 3.4%, 3.6%, 3.8%, 4%, 4.2%, 4.4%, 4.6%, 4.8%, or 5%, but is not limited to the listed values, and other values ​​not listed within the above numerical ranges also apply.

[0018] In aspect 2, the present invention provides a method for producing a pharmaceutical composition comprising: Mixing a metal oxide support with a noble metal precursor and performing an activation treatment to obtain a single atom catalyst. A method for making the single atom catalyst of embodiment 1 is provided.

[0019] Compared with the prior art, the present invention can achieve monoatomic dispersion of precious metals through a one-step impregnation method, significantly increasing the utilization rate of active components, realizing low precious metal usage, improving catalytic activity, and effectively reducing catalyst production costs.

[0020] In a preferred embodiment of the present invention, the mixing method includes incipient wetness impregnation of the metal oxide support in a solution of the noble metal precursor.

[0021] Preferably, the noble metal precursor comprises at least one of tetraammineplatinum nitrate, chloroplatinic acid, palladium chloride, rhodium chloride, tetraamminepalladium nitrate, or rhodium nitrate.

[0022] As a preferred technical solution of the present invention, the method for producing the metal oxide support includes: The method includes calcining a metal oxide precursor to obtain a metal oxide support.

[0023] Preferably, the metal oxide precursor comprises a nitrate salt corresponding to the metal.

[0024] Preferably, the metal oxide precursor comprises cerium nitrate.

[0025] Preferably, the firing temperature is 400 to 600°C, for example, 400°C, 420°C, 440°C, 460°C, 480°C, 500°C, 520°C, 540°C, 560°C, 580°C, or 600°C, and the firing time is 3 to 5 hours, for example, 3 hours, 3.2 hours, 3.4 hours, 3.6 hours, 3.8 hours, 4 hours, 4.2 hours, 4.4 hours, 4.6 hours, 4.8 hours, or 5 hours, but is not limited to the listed values, and other unlisted values ​​within the above numerical ranges also apply.

[0026] In a preferred technical solution of the present invention, drying and polishing treatments are first carried out before the activation treatment.

[0027] Preferably, the temperature of the activation treatment is 300 to 600°C, for example, 300°C, 320°C, 340°C, 360°C, 380°C, 400°C, 420°C, 440°C, 460°C, 480°C, 500°C, 520°C, 540°C, 560°C, 580°C, or 600°C, but is not limited to the listed values, and other values ​​not listed within the above numerical ranges also apply.

[0028] Preferably, the activation treatment time is 120 to 240 minutes, for example, 120 minutes, 140 minutes, 160 minutes, 180 minutes, 200 minutes, 220 minutes, or 240 minutes, but is not limited to the listed values, and other values ​​not listed within the above range also apply.

[0029] Preferably, the activation treatment is carried out in an inert atmosphere.

[0030] Preferably, the pressure condition for the activation treatment is 0.1 to 0.4 MPa, for example, 0.1 MPa, 0.12 MPa, 0.14 MPa, 0.16 MPa, 0.18 MPa, 0.2 MPa, 0.22 MPa, 0.24 MPa, 0.26 MPa, 0.28 MPa, 0.3 MPa, 0.32 MPa, 0.34 MPa, 0.36 MPa, 0.38 MPa, or 0.4 MPa, but is not limited to the listed values, and other values ​​not listed within the above numerical ranges also apply.

[0031] The state of precious metal loading is related to the firing temperature and reaction atmosphere during activation, and in the manufacturing method of the present invention, if activation treatment is performed at a specific temperature in an inert atmosphere, a single atomic loading of precious metal can be formed, simplifying the means for producing the single atom.

[0032] As a preferred technical solution of the present invention, the manufacturing method includes: Putting a metal oxide precursor into a muffle and calcining it, the metal oxide precursor contains a nitrate corresponding to the metal, the nitrate contains cerium nitrate, the temperature is controlled to 400-600°C, and the time is controlled to 3-5 hours to obtain a metal oxide carrier; preparing an impregnation solution containing a precious metal precursor including at least one of tetraammineplatinum nitrate and chloroplatinic acid; Using an incipient wetness impregnation method, take an appropriate amount of the impregnation solution, add the metal oxide support to the impregnation solution, stir and leave it, then put it in an oven for drying treatment to obtain a catalyst precursor supported with a precious metal; The obtained catalyst precursor carrying the precious metal is polished, and then activated in a tubular furnace at a controlled temperature of 300 to 600°C for 120 to 240 minutes under pressure conditions in which the inert atmosphere is maintained at 0.1 to 0.4 MPa, thereby obtaining a single-atom catalyst.

[0033] In a third aspect, the present invention provides a method for producing a pharmaceutical composition comprising: including dehydrogenation of liquid organic hydrogen carriers and heterogeneous catalytic dehydrogenation; The present invention provides a use of the single atom catalyst according to embodiment 1.

[0034] As a preferred technical solution of the present invention, the method for dehydrogenating the liquid organic hydrogen carrier comprises: The method includes mixing a liquid organic hydrogen carrier with the single-atom catalyst according to embodiment 1 to carry out a catalytic dehydrogenation reaction, and obtaining a dehydrogenated product.

[0035] In a preferred technical solution of the present invention, the molar amount of the noble metal single atom in the single atom catalyst is 0.01% to 0.1% of the molar amount of the liquid organic hydrogen carrier, for example, 0.01%, 0.02%, 0.03%, 0.04%, 0.05%, 0.06%, 0.07%, 0.08%, 0.09%, or 0.1%, but is not limited to the listed values, and other values ​​not listed within the above range also apply.

[0036] Preferably, the temperature of the catalytic dehydrogenation reaction is 200 to 400°C, for example, 200°C, 220°C, 240°C, 260°C, 280°C, 300°C, 320°C, 340°C, 360°C, 380°C, or 400°C, but is not limited to the listed values, and other values ​​not listed within the above numerical ranges also apply.

[0037] Preferably, the catalytic dehydrogenation reaction time is 1 to 5 hours, for example, 1 hour, 1.5 hours, 2 hours, 2.5 hours, 3 hours, 3.5 hours, 4 hours, 4.5 hours, or 5 hours, but is not limited to the listed values, and other values ​​not listed within the above range also apply.

[0038] Preferably, the catalytic dehydrogenation reaction is carried out in an inert atmosphere.

[0039] Preferably, the pressure condition for the catalytic dehydrogenation reaction is 0.1 to 1 MPa, for example, 0.1 MPa, 0.2 MPa, 0.3 MPa, 0.4 MPa, 0.5 MPa, 0.6 MPa, 0.7 MPa, 0.8 MPa, 0.9 MPa, or 1 MPa, but is not limited to the listed values, and other values ​​not listed within the above ranges also apply.

[0040] Preferably, the liquid organic hydrogen carrier comprises dibenzyltoluene.

[0041] The single-atom catalyst of the present invention is not limited to use with dibenzyltoluene, but rather has a commonality with catalysts for dehydrogenation of aromatic rings, and the greater the number of benzene rings, the more difficult the dehydrogenation becomes. Therefore, the single-atom catalyst of the present invention is applicable to dibenzyltoluene, which means that it can also be used with other low-benzene ring organic liquids. Therefore, common organic liquids such as methylcyclohexane and decahydronaphthalene can all be dehydrogenated as liquid organic hydrogen carriers using the single-atom catalyst of the present invention. [Effects of the Invention]

[0042] Compared with the prior art solutions, the present invention has at least the following beneficial effects:

[0043] The present invention constructs and applies the single-atom catalyst to the dehydrogenation reaction process of liquid organic hydrogen carriers. Compared with metal particles, the single-atom catalyst exhibits superior catalytic activity, effectively reduces the amount of precious metal used, and reduces catalyst costs.

[0044] In particular, when the obtained single-atom catalyst is applied to the dehydrogenation of perhydrodibenzyltoluene, the dehydrogenation degree of the single-atom catalyst of the present invention is comparable to that of the conventional Pt / Al2O3 catalyst, but the amount of precious metal used is correspondingly reduced, the utilization rate of the active component is increased, and the cost of the catalyst is reduced. DETAILED DESCRIPTION OF THE INVENTION

[0045] The technical solution of the present invention will be further described below through specific embodiments.

[0046] Those skilled in the art should understand that the above examples are only for understanding the present invention and should not be considered as specifically limiting the present application. [Example]

[0047] This example provides a single-atom catalyst for dehydrogenating liquid organic hydrogen carriers, and the preparation method of the single-atom catalyst includes the following steps:

[0048] Cerium nitrate, a metal oxide precursor, was placed in a muffle and calcined at a controlled temperature of 600°C for 2 hours to obtain a metal oxide support.

[0049] An impregnation solution was prepared using chloroplatinic acid, a precious metal precursor.

[0050] The incipient wetness impregnation method was adopted, and an appropriate amount of the impregnation solution was taken, and the metal oxide support was added to the impregnation solution, and the mixture was stirred uniformly and allowed to stand for 12 hours. After that, the mixture was placed in an oven and dried at 120°C for 12 hours to obtain a catalyst precursor loaded with precious metals.

[0051] The obtained catalyst precursor carrying the precious metal was polished and then activated in a tubular furnace. The temperature was controlled at 600°C and the N2 atmosphere was maintained at 0.25 MPa for 180 min to obtain a monoatomic catalyst with a monoatomic Pt loading of 0.5%. [Example]

[0052] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the activation temperature was changed from 600°C to 300°C. [Example]

[0053] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the activation temperature was changed from 600°C to 400°C. [Example]

[0054] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the activation temperature was changed from 600°C to 500°C. [Example]

[0055] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the activation temperature was adjusted from 600°C to 650°C. [Example]

[0056] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the mass concentration of the noble metal precursor was adjusted so that the loading amount of single-atom Pt in the obtained single-atom catalyst was 0.5% to 0.3%. [Example]

[0057] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the mass concentration of the noble metal precursor was adjusted so that the loading amount of single-atom Pt in the obtained single-atom catalyst was 0.5% to 0.1%. [Example]

[0058] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst was the same as that of Example 1, except that the mass concentration of the noble metal precursor was adjusted so that the loading amount of single-atom Pt in the obtained single-atom catalyst was 0.5% to 1%. [Example]

[0059] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The preparation method of the single-atom catalyst is the same as that of Example 1, except that the metal oxide support in the obtained single-atom catalyst is changed from CeO2 to ZrO2. [Example]

[0060] This example provides a single-atom catalyst for dehydrogenation of liquid organic hydrogen carriers. The manufacturing method of the single-atom catalyst was the same as that of Example 1, except that the metal oxide support in the obtained single-atom catalyst was changed from CeO2 to TiO2.

[0061] In this comparative example, a catalyst was provided, and the activation treatment of the catalyst manufacturing method was performed by polishing the obtained catalyst precursor carrying a noble metal, followed by activation treatment in a tubular furnace, controlling the temperature to 400°C, and maintaining the pressure of pure hydrogen gas (H) at 0.25 MPa for 60 minutes to obtain a catalyst carrying aggregated Pt. The other conditions were exactly the same as in Example 1. Control Group 1

[0062] This control group provided a catalyst, and the manufacturing method of the catalyst included impregnating Pt into an Al2O3 support using an incipient wetness impregnation method, controlling the Pt loading to 1 wt.%, and then activating the catalyst obtained by impregnation in a tubular furnace under the same activation conditions as in Comparative Example 1 to obtain a 1Pt / Al2O3 catalyst.

[0063] This application example provides a method for dehydrogenating a liquid organic hydrogen carrier, the method including the following steps:

[0064] 0.8g of the catalyst obtained in Example 1 was placed in a batch reactor containing 15g of perhydrodibenzyltoluene, a liquid organic hydrogen carrier. The molar amount of the precious metal in the catalyst was controlled to be 0.037% of the molar amount of the liquid organic hydrogen carrier. Nitrogen gas was first introduced to replace the gas in the reaction system. After the air was removed, the atmospheric pressure was maintained at 0.1MPa and controlled using a programmable temperature controller. When the set temperature reached 290°C, the dehydrogenation reaction was started to time. After 3 hours, the reaction was stopped and cooled to room temperature. The liquid phase product was collected and analyzed. The analytical equipment used was a chromatograph equipped with a TCD detector, and online detection was performed to obtain data on the dehydrogenated product. Application Examples 2 to 10

[0065] Application Examples 2 to 10 provide methods for dehydrogenating a liquid organic hydrogen carrier, respectively. The methods were identical to Application Example 1 except that the catalysts of Examples 2 to 10 were used instead of the catalyst of Example 1, and the molar amount of the precious metal in the catalyst relative to the molar amount of the liquid organic hydrogen carrier was controlled to 0.037%, the same as Application Example 1, and the other conditions were the same. Comparative Application Example 1

[0066] These comparative application examples provide methods for dehydrogenating liquid organic hydrogen carriers, and the methods were identical to application example 1 except that the catalysts of comparative example 1 were used instead of the catalysts of example 1, and the molar amount of the precious metal in the catalyst relative to the molar amount of the liquid organic hydrogen carrier was controlled to 0.037%, the same as application example 1, and the other conditions were the same as application example 1.

[0067] These comparative application examples provide methods for dehydrogenating liquid organic hydrogen carriers. The methods were identical to those in Application Example 1, except that the catalysts in Control Group 1 were used instead of the catalysts in Example 1, the amount of catalyst used was kept at 0.8 g, and the molar amount of precious metal in the catalyst relative to the molar amount of the liquid organic hydrogen carrier was 0.075%.

[0068] The dehydrogenation results of the relevant catalysts are shown in Table 1 below. [Table 1]

[0069] As can be seen from Table 1, a comparison of Application Example 1 and Comparative Application Example 1, performed in a batch reactor at a reaction temperature of 290°C for 3 hours, revealed that Application Example 1 had significant dehydrogenation activity. This also indicates that dehydrogenation activity is determined by the state of the metal species, with the dehydrogenation ability of monatomic species being superior to that of aggregated metal clusters. In Applications 1-5, the effect of activation temperature on reaction activity was examined. It was found that high or low activation temperatures affected the distribution ability of monatomic species, and an optimal activation temperature existed. An appropriate activation temperature favors the dispersion of metal species at the monatomic level, but too low a reaction temperature results in insufficient dispersion, while too high a reaction temperature leads to aggregation of the active components. In Applications 6-8, the effect of the amount of precious metal used on dehydrogenation reaction activity was examined. It was found that an optimal metal loading existed. Low metal loading resulted in over-dispersion of the active sites, resulting in insufficient activation ability for the reactants, while high metal loading limited the dispersion ability of monatomic species to a certain extent. By comparing Application Example 1 with Application Examples 8 and 9 and examining the influence of different oxide supports on the dehydrogenation activity, it can be seen that this embodiment is applicable to different oxide supports, all of which have high dehydrogenation activity. Compared with the catalyst of Control Group 1 (conventional Pt / Al2O3), the dehydrogenation degree of the single-atom catalyst of the present invention is comparable to that of the catalyst of Control Group 1, but the amount of precious metal used is correspondingly reduced, which increases the utilization rate of the active component and reduces the catalyst cost.

[0070] Although the present invention has been described in detail with reference to the above examples, the present invention is not limited to the above detailed structural features, i.e., it does not mean that the present invention must be implemented depending on the above detailed structural features. Those skilled in the art should understand that any improvements to the present invention, equivalent replacement of components used in the present invention, addition of auxiliary components, selection of specific forms, etc., are all within the scope of protection and disclosure of the present invention.

[0071] Although the preferred embodiments of the present invention have been described in detail above, the present invention is not limited to the specific contents of the above embodiments. Various simple modifications can be made to the technical solutions of the present invention within the scope of the technical idea of ​​the present invention, and all of these simple modifications fall within the scope of the claims of the present invention.

[0072] It should be noted that the specific technical features described in the above specific embodiments can be combined in any appropriate manner unless there is a contradiction, and in order to avoid unnecessary duplication, the present invention does not specifically describe various possible combinations.

[0073] Furthermore, various different embodiments of the present application can be arbitrarily combined, and should be considered as the disclosure of the present invention as long as they do not violate the spirit of the present invention.

Claims

1. A catalyst comprising a metal oxide support and a noble metal monatom supported on the oxide support. A single-atom catalyst for use in dehydrogenation of a liquid organic hydrogen carrier, characterized in that:

2. the metal oxide support comprises a transition metal oxide and / or a rare earth metal oxide; Preferably, the metal oxide support comprises any one of cerium oxide, titanium oxide, or zirconium oxide; Preferably, the noble metal comprises at least one of Pt, Pd, or Rh; Preferably, the amount of the noble metal monoatom supported is 0.1% to 5% based on the mass of the metal oxide support being 100%.

2. The single atom catalyst of claim 1.

3. 3. A method for producing the single atom catalyst according to claim 1 or 2, comprising: Mixing a metal oxide support with a noble metal precursor and performing an activation treatment to obtain a single atom catalyst.

1. A method for producing a single-atom catalyst, comprising:

4. The mixing method includes incipient wetness impregnation of the metal oxide support in a solution of the precious metal precursor; Preferably, the noble metal precursor comprises at least one of tetraammineplatinum nitrate or chloroplatinic acid. The method for producing a single atom catalyst according to claim 3 .

5. The method for producing the metal oxide support includes the steps of: calcining the metal oxide precursor to obtain a metal oxide support; Preferably, the metal oxide precursor comprises a nitrate salt corresponding to the metal; Preferably, the metal oxide precursor comprises cerium nitrate; Preferably, the firing temperature is 400 to 600°C and the firing time is 3 to 5 hours. The method for producing a single atom catalyst according to claim 3 .

6. Before the activation treatment, a drying and polishing treatment is first performed, Preferably, the activation treatment temperature is 300 to 600°C, Preferably, the activation treatment time is 120 to 240 min, Preferably, the activation treatment is carried out in an inert atmosphere, Preferably, the pressure condition of the activation treatment is 0.1 to 0.4 MPa.

4. The method for producing a single atom catalyst according to claim 3.

7. A metal oxide precursor is placed in a muffle and calcined, the metal oxide precursor containing a nitrate corresponding to the metal, the nitrate containing cerium nitrate, the temperature is controlled to 400-600°C, and the time is controlled to 3-5 hours to obtain a metal oxide support; preparing an impregnation solution containing a precious metal precursor including at least one of tetraammineplatinum nitrate and chloroplatinic acid; Using an incipient wetness impregnation method, take an appropriate amount of the impregnation solution, add the metal oxide support to the impregnation solution, stir and leave it, then put it in an oven for drying treatment to obtain a catalyst precursor supported with a precious metal; The obtained catalyst precursor carrying the precious metal is polished, and then activated in a tubular furnace, controlling the temperature to 300 to 600°C and maintaining the inert atmosphere at a pressure of 0.1 to 0.4 MPa for 120 to 240 minutes, to obtain a single-atom catalyst.

4. The method for producing a single atom catalyst according to claim 3.

8. Use of the single atom catalyst according to claim 1 or 2, Dehydrogenation of a liquid organic hydrogen carrier, 1. Use of a single atom catalyst, characterized in that:

9. The method for dehydrogenating the liquid organic hydrogen carrier comprises: Mixing a liquid organic hydrogen carrier with the single-atom catalyst to carry out a catalytic dehydrogenation reaction and obtain a dehydrogenated product. Use of the single atom catalyst according to claim 8.

10. the molar amount of the noble metal single atom in the single atom catalyst is 0.01% to 0.1% of the molar amount of the liquid organic hydrogen carrier; Preferably, the temperature of the catalytic dehydrogenation reaction is 200 to 400°C; Preferably, the catalytic dehydrogenation reaction time is 1 to 5 hours, Preferably, the catalytic dehydrogenation reaction is carried out in an inert atmosphere; Preferably, the pressure condition of the catalytic dehydrogenation reaction is 0.1 to 1 MPa, Preferably, the liquid organic hydrogen carrier comprises at least one of dibenzyltoluene, methylcyclohexane, or decahydronaphthalene. Use of the single atom catalyst according to claim 9.

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