Catalyst coating body, reactor, application of catalyst coating body and reactor, and organic hydride dehydrogenation method

Abstract

The invention relates to the field of catalytic reaction equipment, and discloses a catalyst coating body, a reactor, application of the catalyst coating body and an organic hydride dehydrogenation method.The catalyst coating body comprises a shell and a cavity formed by the shell in a surrounding mode, a heating body is arranged in the cavity, the surface of the shell is coated with a catalyst in the length direction, the shell is a non-uniform-section body, and the heating body is arranged in the cavity. The shell comprises small-section sections at the two ends and a large-section section arranged between the small-section sections at the two ends. The reactor has the advantages of being good in heat transfer effect, uniform in temperature distribution, capable of avoiding quick loss of active substances and suitable for large-scale industrial production.

Description

Technical Field

[0001] The invention relates to a catalytic reaction device, in particular to a catalyst coating body and a reactor and applications thereof and a method for dehydrogenating organic hydrides. Background Art

[0002] Today, the refining industry faces challenges in many aspects of its operations. On the one hand, strict environmental regulations such as the European Emissions Trading System require refineries to reduce on-site greenhouse gas emissions. On the other hand, the demand for diesel and gasoline is steadily increasing, and stricter requirements for sulfur content in automotive fuels are also forcing crude oil to be more thoroughly refined, which has led to a rapid increase in the demand for energy and hydrogen in refineries. The most common hydrogen production route in refineries is steam reforming of light hydrocarbons, which produces 25% of the industry's total carbon dioxide emissions. At the same time, the refining and chemical industries mostly rely on fossil fuels for energy, which also causes a large amount of greenhouse gas and harmful substances emissions. Renewable energy can now meet about 20% of the world's energy needs, but the instability of renewable energy due to climate conditions and regional differences makes it difficult to transmit and distribute the electricity generated by renewable energy through the power grid.

[0003] Liquid organic hydrogen carriers (LOHC) can store hydrogen under ambient conditions and are low-cost, safe and easy to manage. In addition, this technology allows long-term storage and simple transportation of hydrogen without evaporation or other hydrogen losses. The storage of hydrogen in LOHC is usually based on the reversible hydrogenation and dehydrogenation of carbon double bonds. During the hydrogenation process, the double bonds are saturated with hydrogen and heat is released; dehydrogenation mainly involves the removal of hydrogen from saturated hydrocarbons to regenerate double bonds, which requires the absorption of heat. The heat required for the traditional dehydrogenation of organic hydrides needs to be transferred from the flue gas generated by fossil energy fuels to the catalyst through the reactor shell. While producing carbon dioxide, the poor heat transfer effect will also lead to excessive temperature differences in various parts of the reactor, affecting the reaction effect.

[0004] Using electric energy to release the hydrogen stored in LOHC can be one of the important ways to solve the problem of carbon dioxide emissions in the field of oil refining and chemical industry and achieve carbon peak and carbon neutrality. The invention of CN116440925A provides a structured catalyst with conductive properties, including a conductive skeleton and an active substance loaded on the surface of the conductive skeleton; during the reaction process, the electric heat generated by the constructed structured catalyst can be continuously and efficiently transferred to the active site, strengthening the heat transfer process in the reaction, and greatly increasing the energy efficiency. Moreover, its energy comes from green electricity generated by renewable energy, the whole process of catalytic reaction is pollution-free, and it can efficiently realize the conversion of renewable energy into chemical energy, and has broad application prospects in green and efficient energy storage and chemical production. However, this structured catalyst has poor mechanical properties and fast loss of active substances, and is not suitable for large-scale industrial production. Summary of the invention

[0005] The purpose of the present invention is to overcome the problem that poor heat transfer effect affects the reaction effect in the prior art, and to provide a catalyst coating body and a reactor and their application and a method for dehydrogenating organic hydrides, which have the advantages of good heat transfer effect, uniform temperature distribution, ability to avoid rapid loss of active substances, and suitability for large-scale industrial production.

[0006] In order to achieve the above object, the present invention provides a catalyst-coated body on one hand, wherein the catalyst-coated body comprises:

[0007] The shell and the cavity formed by the shell have a heating body in the cavity, and the shell surface is coated with a catalyst along the length direction, wherein the shell is a non-uniform cross-section body, and the shell includes small cross-section sections at both ends and a large cross-section section arranged between the small cross-section sections at both ends.

[0008] A second aspect of the present invention provides a reactor, wherein a plurality of catalyst-coated bodies according to the present invention are arranged in a reaction chamber of the reactor, and an axis of each catalyst-coated body is parallel to the axis of the reaction chamber.

[0009] The third aspect of the present invention provides the use of the catalyst-coated body of the present invention and / or the reactor of the present invention in an endothermic reaction, preferably in a dehydrogenation reaction.

[0010] A fourth aspect of the present invention provides a method for dehydrogenating an organic hydride, the method using the reactor of the present invention, comprising coating a dehydrogenation catalyst on the catalyst coating body, and introducing an organic hydride into a reaction chamber.

[0011] Through the above technical scheme, by providing a heating body in the shell, coating the catalyst on the surface of the shell, and arranging different cross-sectional segments along the length direction of the shell, the heat transfer effect can be enhanced while avoiding the problem of excessive local temperature difference in the reaction, and the distribution amount of the catalyst can be controlled; further, when applied to dehydrogenation reactions, it has the advantages of no carbon emissions, low energy consumption, uniform temperature distribution of the reaction system, and small pressure drop. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 It is a schematic diagram of the structure of the reactor of some embodiments of the present invention;

[0013] Figure 2 yes Figure 1 a bottom view of the reactor shown;

[0014] Figure 3 yes Figure 1 Schematic diagram of a catalyst-coated body;

[0015] Figure 4 yes Figure 1 Schematic diagram of the three-dimensional structure of the raw material distributor;

[0016] Figure 5 It is a structural schematic diagram of a raw material distributor in the prior art.

[0017] Description of Reference Numerals

[0018] 1 reactor; 11 feed inlet; 12 discharge outlet; 13 catalyst coating body; 14 raw material distributor. DETAILED DESCRIPTION

[0019] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0020] The endpoints and any values ​​of the ranges disclosed in this article 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 each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0021] In the present invention, unless otherwise specified, directional words such as "up, down, top, bottom" are usually used with reference to the directions shown in the drawings or are used to describe the relative positional relationships of components in the vertical, perpendicular or gravity direction. "Inside and outside" refer to the inside and outside relative to the outline of each component itself. The cross-section in the present invention refers to the cross-section of the horizontal plane.

[0022] In one aspect, the present invention discloses a catalyst-coated body, such as Figure 3 As shown, the catalyst coating body 13 comprises:

[0023] The shell and the cavity formed by the shell, a heating body is arranged in the cavity, and the surface of the shell is coated with a catalyst along the length direction, wherein the shell is a non-uniform cross-section body, and the shell includes a small cross-section section located at both ends and a large cross-section section arranged between the small cross-section sections at both ends, and there is a smooth transition between the large cross-section section and the small cross-section section. In this way, a heating body is arranged in the shell, and the catalyst is coated on the surface of the shell, and the heat required for the reaction is transferred from the heating body to the catalyst, which can enhance the heat transfer effect, on the one hand, avoid the problem of excessive local temperature difference in the reaction, and on the other hand, avoid the problem of rapid loss of active substances in the catalyst. In addition, different cross-section sections are arranged along the length direction of the shell, and the content of the catalyst can be controlled in the medium volume area of ​​the reactor; further, it is applied to the dehydrogenation reaction, and has the advantages of no carbon emissions, low energy consumption, uniform temperature distribution of the reaction system, and small pressure drop.

[0024] In some embodiments of the present invention, the coating thickness of the catalyst on the shell surface is 0.1-1 mm.

[0025] In some embodiments of the present invention, the shell includes a non-coated portion and a coated portion coated with a catalyst, wherein the cross-sectional area of ​​the shell at the junction of the non-coated portion and the coated portion is larger than that at the end portion. Thus, the amount of catalyst used is reduced, the temperature in the reactor is made more uniform, and the occurrence of side reactions can be reduced, and the stability of the system is improved. The non-coated portion is used for preheating the raw materials, and the raw materials also need a certain amount of space after passing through the distributor to achieve uniform distribution. Full-area coating will lead to a waste of catalysts, and will also cause the actual reaction temperature of some raw materials to be too low, which is prone to side reactions and carbon deposition.

[0026] In some embodiments of the present invention, the cross-sectional area of ​​the shell preferably decreases from the junction of the non-coated portion and the coated portion toward both ends.

[0027] In some embodiments of the present invention, the length of the coating portion is preferably 60-80% of the length of the reaction chamber. The main function of the non-coating section is to preheat the raw material. The temperature at which the raw material begins to contact the catalyst is positively correlated with the length of the non-coating section. This range can make the temperature in the reactor more uniform.

[0028] In some embodiments of the present invention, Figure 3 As shown, the heating body is configured as a heating rod with the same shape as the shell, and the shell is covered on the outside of the heating rod. It can be understood that the heating rod and the shell have the same shape but different sizes, so that the shell can cover and fit the heating rod. The shell is made of heat-conductive material with a thermal conductivity of 25-35K, which can improve the heat transfer efficiency and better achieve temperature control.

[0029] In some embodiments of the present invention, the material of the shell is selected from at least one of alumina ceramics, barium titanate ceramics, silicon carbide ceramics, or magnesium oxide ceramics. It should be noted that the reasons for the rapid loss of active substances in the prior art include insufficient mechanical strength of the conductive skeleton or the shell or weak bonding with the active substance. The present invention selects a specific shell material and a coating slurry material so that the shell can have sufficient mechanical properties and enhance the bonding ability between the shell and the active substance.

[0030] In some embodiments of the present invention, the heating rod is an electric heating rod, so that the energy required for the reaction can be derived from green electricity generated by renewable energy. In this way, the whole process of the catalytic reaction is pollution-free, and the conversion of renewable energy into chemical energy can be efficiently realized, which has broad application prospects in green and efficient energy storage and chemical production. In particular, the heat required for the dehydrogenation of traditional organic hydrides needs to be transferred to the catalyst by the flue gas generated by fossil energy fuels through the reactor shell. While generating carbon dioxide, the temperature difference in various places in the reactor is too large due to poor heat transfer effect, which affects the reaction effect. The catalyst-coated body of the present invention is applied to the dehydrogenation reaction, which has the advantages of no carbon emissions, low energy consumption, and uniform temperature distribution of the reaction system.

[0031] In order to coat the catalyst as evenly as possible, the outer contour of the cross section of the heating body and the shell can be a circle, an ellipse or a ring formed by a multi-segment line. When the cross section is formed by a multi-segment line, the adjacent line segments have a smooth transition. In some embodiments of the present invention, the shell is a cylinder with a circular cross section, and the ratio of the maximum diameter to the minimum diameter of the shell is preferably 1.3-3. This has the effect of reducing the temperature difference in the reaction section.

[0032] Based on the above disclosure, the present invention provides a reactor, such as Figure 1 As shown, a plurality of catalyst coating bodies 13 of the present invention are arranged in the reaction chamber of the reactor 1, and the axis of each catalyst coating body 13 is parallel to the axis of the reaction chamber. In this way, the reactor adopts the catalyst coating body of the present invention, which can solve the problem of excessive local temperature difference in the reactor and facilitate large-scale industrial production.

[0033] In some embodiments of the present invention, the catalyst coating body 13 is arranged in the reaction chamber so that the raw material contacts the non-coating part first and then contacts the coating part. In other words, when the catalyst coating body 13 is installed in the reaction chamber, the coating part is located below the non-coating part.

[0034] In some embodiments of the present invention, a raw material distributor 14 is provided in the reactor 1. Preferably, the raw material distributor 14 is provided at the top of the reaction chamber, and the coated portion of the catalyst-coated body is close to the raw material distributor. The cross-sectional area of ​​the shell decreases from the junction of the non-coated portion and the coated portion to both ends. In this way, the coating area of ​​the catalyst gradually expands along the feed direction, and the heat transfer area is also the same. The raw material is evenly diffused from the top raw material distributor to the reaction chamber of the reactor, which can further improve the reaction effect.

[0035] To further evenly distribute the catalyst and heat in the reaction chamber, in some embodiments of the present invention, Figure 2 As shown, a plurality of catalyst coating body rings are arranged in the reaction chamber, and the plurality of catalyst coating body rings are arranged at equal intervals along the radial direction of the reaction chamber, and each catalyst coating body ring includes catalyst coating bodies 13 arranged at equal intervals along the circumference of the reaction chamber.

[0036] In some embodiments of the present invention, the feed port 11 and the discharge port 12 of the reactor 1 are respectively connected to the two ends of the reaction chamber, and preferably the feed port 11 is connected to the top of the reaction chamber and is connected to the feed port of the raw material distributor 14. In this way, the raw material is uniformly diffused into the reactor from the top feed port 11 through the raw material distributor, and the product gas is discharged from the discharge port 12 at the other end after contacting with the catalyst.

[0037] In some embodiments of the present invention, the raw material distributor 14 is configured as a gas distributor, including a hemispherical distributor connected to the feed port 11 of the reactor 1, the hemispherical distributor is provided with a plurality of distribution holes, and an impeller is installed in each distribution hole. Thus, the uniformity of raw material distribution is improved while reducing the pressure drop of the distributor and the manufacturing cost.

[0038] The present invention provides the use of the catalyst coating body 13 of the present invention and / or the reactor 1 of the present invention in an endothermic reaction, preferably in a dehydrogenation reaction. The present invention can make the maximum temperature difference in the reactor 10-35°C and the reaction gas inlet and outlet pressure difference 5-20Kpa.

[0039] Based on the above disclosure, the present invention provides a method for dehydrogenating an organic hydride. The method uses the reactor 1 of the present invention, and includes coating a dehydrogenation catalyst on a catalyst coating body 13 and introducing an organic hydride into a reaction chamber.

[0040] The heat required for traditional dehydrogenation of organic hydrides needs to be transferred from the flue gas generated by fossil energy fuels to the catalyst through the reactor shell. While producing carbon dioxide, the poor heat transfer effect will cause excessive temperature differences in various parts of the reactor, affecting the reaction effect.

[0041] The present invention aims at the problems of carbon dioxide emission in the dehydrogenation process of organic hydrogen carrier and excessive local temperature difference in the reactor in the prior art. When used for the dehydrogenation of organic liquid hydrogen carrier, the present invention has the advantages of no carbon emission, low energy consumption, uniform temperature distribution of the reaction system, small pressure drop, etc.

[0042] To further improve the dehydrogenation effect, in some embodiments of the present invention, the organic hydride is fed into the reaction chamber through the raw material distributor 14 .

[0043] In some embodiments of the present invention, the reaction conditions include: reaction pressure of 0-0.5 MPa, temperature of 220-380°C, mass space velocity of 0.1-10 h -1 .

[0044] In the present invention, there is no special requirement for the organic hydride, and commonly used organic hydrides can be used in the present invention. The following exemplary description is not intended to limit the scope of the present invention. In some embodiments of the present invention, the organic hydride includes at least one of methylcyclohexane, cyclohexane, tetralin, decalin, perhydroethylcarbazole and perhydrocarbazole.

[0045] In the present invention, there is no special requirement for the dehydrogenation catalyst, and the commonly used dehydrogenation catalyst of organic hydride can be used in the present invention. The following exemplary description is not intended to limit the scope of the present invention. In some embodiments of the present invention, the dehydrogenation catalyst comprises, by weight: 0.1% to 1% of an active component, 0.3% to 2% of an auxiliary agent, and 97% to 99.6% of a carrier, wherein the active component comprises one or more of Pt, Pd, Rh, Ru and Au; the auxiliary agent comprises one or more of chromium, molybdenum, tungsten, vanadium, niobium and tantalum; and the carrier comprises one or more of alumina, zirconium oxide and silicon-aluminum molecular sieve.

[0046] In the present invention, there is no special requirement for how to coat the catalyst onto the shell, and commonly used coating methods can be used in the present invention. The following exemplary description does not limit the scope of the present invention. In some embodiments of the present invention, coating a dehydrogenation catalyst on the catalyst-coated body 13 includes: pretreating the outer shell of the catalyst-coated body 13 using existing technology, coating the coating slurry onto the shell surface of the catalyst-coated body 13 using a quantitative coating device in the prior art, and then drying and placing it in a muffle furnace for calcination.

[0047] In some embodiments of the present invention, coating is preferably performed along the feeding direction of the organic hydride in the reactor 1 .

[0048] In some embodiments of the present invention, preferred drying conditions include: temperature 80-120° C., time 3-8 h.

[0049] In some embodiments of the present invention, preferred calcination conditions include: temperature 300-400° C., time 3-6 h.

[0050] In the present invention, there are no special requirements for the preparation of the coating slurry, and the commonly used coating slurry preparation methods can be used in the present invention. The following exemplary description shows that in some embodiments of the present invention, the preparation of the coating slurry includes: adding deionized water to the dehydrogenation catalyst and stirring it thoroughly, adding a binder and a dispersant and ball milling them with a ball mill, and mixing them to form a coating slurry, wherein the mass ratio of dehydrogenation catalyst: deionized water: binder: dispersant is 1:10-1000:0.1-0.5:0.1-0.5.

[0051] In the present invention, there is no special requirement for the binder, and commonly used binders can be used in the present invention. The following exemplary description shows that in some embodiments of the present invention, the binder is one or more of aluminum dihydrogen phosphate, methyl cellulose and polyvinyl alcohol.

[0052] In the present invention, there is no special requirement for the dispersant, and commonly used dispersants can be used in the present invention. The following exemplary description shows that in some embodiments of the present invention, the dispersant is one or more of polyethylene glycol, ethanolamine, polydextrose and carboxymethyl cellulose.

[0053] The advantages of the present invention will be described below by way of examples, but the present invention is not limited thereto.

[0054] Example 1

[0055] This embodiment adopts Figure 1-Figure 3 The reactor shown in the figure has a discharge port 12 at the bottom of the reactor 1, and a feed port 11 is connected to a gas distributor. The gas distributor includes a hemispherical distribution body connected to the top wall of the reaction chamber, and a plurality of distribution holes are opened on the hemispherical distribution body, and an impeller is installed in each distribution hole.

[0056] A plurality of catalyst-coated bodies 13 are provided in the reaction chamber, the axis of each catalyst-coated body 13 is arranged parallel to the axis of the reaction chamber, the coated portion of the catalyst-coated body is located above the non-coated portion and is arranged close to the gas distributor; a plurality of catalyst-coated body rings are provided in the reaction chamber, the plurality of catalyst-coated body rings are arranged at equal intervals along the radial direction of the reaction chamber, and each catalyst-coated body ring includes catalyst-coated bodies arranged at equal intervals along the circumference of the reaction chamber.

[0057] The catalyst coating body 13 includes an electric heating rod and a shell that is fitted and coated on the outside of the electric heating rod. Along the length direction, the shell includes a non-coated portion and a coated portion coated with a catalyst, wherein the cross-sectional area of ​​the shell at the junction of the non-coated portion and the coated portion gradually decreases toward the end;

[0058] The length of the catalyst coating body 13 is the same as the length of the reaction chamber. The shell is made of alumina ceramics coated with 0.4 wt% Pt-Mo / Al 2 O3 The catalyst, the length of the coating portion is 70% of the length of the catalyst coating body, the ratio of the maximum diameter to the minimum diameter on the catalyst coating body is 2, and the coating thickness of the catalyst is 1 mm. The specific operation steps are as follows: pre-treat the shell of the catalyst coating body 13 with 0.4wt% acetic acid as a pre-treating agent, wash with water to neutrality after acid treatment, dry and weigh for use; 2 O 3 The catalyst powder was added to deionized water and stirred thoroughly, and methylcellulose and polyethylene glycol were added and ground in a ball mill. 2 O 3 The mass ratio of catalyst powder: deionized water: methyl cellulose: polyethylene glycol is 1:99:0.3:0.4. The coating slurry is coated from the feed direction of the reactor using a quantitative coating device. After coating, it is dried in a 90°C oven for 4 hours, placed in a muffle furnace and calcined at 350°C for 4 hours, and then taken out.

[0059] The processed catalyst coating body 13 is installed on the reactor, and the reaction system is heated to 300°C by power. The raw material gas containing cyclohexane (cyclohexane content 99.5%) is introduced. The reaction inlet pressure is 0.3 MPa, and the reaction mass space velocity is 4 h -1 The maximum reaction temperature of the reaction zone was set to 300°C, and direct contact reaction was performed. The minimum temperature of the catalyst coating portion in the reactor and the pressure difference between the inlet and outlet of the reaction gas were measured. The products after the reaction were analyzed by gas chromatography. The results are shown in Table 1.

[0060] Example 2

[0061] The difference from Example 1 is that 0.2 wt% Pt-Mo / Al is coated 2 O 3 The catalyst, the length of the coating part is 60% of the length of the catalyst coating body, the shell material is barium titanate ceramic, the ratio of the maximum diameter to the minimum diameter on the catalyst coating body is 1.5, and the coating thickness of the catalyst is 0.3mm. The processed catalyst coating body 13 is installed on the reactor, the reaction system is heated to 250°C by power, and the raw material gas containing perhydrocarbazole (perhydrocarbazole content 99.5%) is introduced, the reaction inlet pressure is 0.5MPa, and the reaction mass space velocity is 8h -1 The maximum reaction temperature of the reaction zone was set to 250°C, and direct contact reaction was performed. The minimum temperature of the catalyst coating portion in the reactor and the pressure difference between the inlet and outlet of the reaction gas were measured. The products after the reaction were analyzed by gas chromatography. The results are shown in Table 1.

[0062] Example 3

[0063] The difference from Example 1 is that 0.8 wt% Pt-Mo / Al is coated 2 O3 The catalyst, the length of the coating portion is 80% of the length of the catalyst coating body, the shell material is silicon carbide ceramic, the ratio of the maximum diameter to the minimum diameter on the catalyst coating body is 3, and the coating thickness of the catalyst is 0.6mm. The processed catalyst coating body 13 is installed on the reactor, and the reaction system is heated to 350°C by power, and the raw material gas containing decalin (decalin content 99%) is introduced, the reaction inlet pressure is 0.5MPa, and the reaction mass space velocity is 1h -1 The maximum reaction temperature of the reaction zone was set to 350°C, and direct contact reaction was performed. The minimum temperature of the catalyst coating portion in the reactor and the pressure difference between the inlet and outlet of the reaction gas were measured. The products after the reaction were analyzed by gas chromatography. The results are shown in Table 1.

[0064] Example 4

[0065] Different from Example 1, the length of the coating portion is 100% of the length of the catalyst coating body, and the ratio of the maximum diameter to the minimum diameter of the heating rod is 4.

[0066] Example 5

[0067] The difference from Example 1 is that the prior art is used as Figure 5 Gas distributor shown.

[0068] Comparative Example 1

[0069] The same amount of 0.4 wt% Pt-Mo / Al as in Example 1 was loaded into a tube-type fixed bed reactor in the prior art. 2 O 3 The catalyst was diluted with an inert filler, and cyclohexane raw gas was introduced under conventional flue gas heating. The reaction conditions were the same as in Example 1. The results are shown in Table 1.

[0070] Comparative Example 2

[0071] Different from Example 1, the catalyst-coated body is configured as a body of uniform cross-section, that is, a cylinder with a constant diameter along the length direction.

[0072] Table 1

[0073]

[0074] The preferred embodiments of the present invention are described in detail above in conjunction with the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various specific technical features in any appropriate manner. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A catalyst-coated body, characterized in that: The catalyst-coated body (13) comprises: The shell and the cavity formed by the shell have a heating body in the cavity, and the shell surface is coated with a catalyst along the length direction, wherein the shell is a non-uniform cross-section body, and the shell includes small cross-section sections at both ends and a large cross-section section arranged between the small cross-section sections at both ends.

2. The catalyst-coated body according to claim 1, characterized in that The shell comprises a non-coating portion and a coating portion coated with a catalyst, wherein the cross-sectional area of ​​the shell at the junction of the non-coating portion and the coating portion is larger than that of the end portion; Preferably, the cross-sectional area of ​​the shell decreases from the junction of the non-coated portion and the coated portion to both ends; and / or Preferably, the length of the coating portion is 60-80% of the length of the reaction chamber.

3. The catalyst-coated body according to claim 1 or 2, characterized in that The heating body is configured as a heating rod having the same shape as the shell, the shell is coated on the outside of the heating rod, and the heating rod is preferably an electric heating rod; and / or The cross section of the shell is circular, and preferably the ratio of the maximum diameter to the minimum diameter of the shell is 1.3-3; and / or The thermal conductivity of the shell is 25-35K; and / or The material of the shell is selected from at least one of alumina ceramics, barium titanate ceramics, silicon carbide ceramics or magnesium oxide ceramics; and / or The coating thickness of the catalyst on the shell surface is 0.1-1 mm.

4. A reactor, characterized in that: A plurality of catalyst-coated bodies (13) according to any one of claims 1 to 3 are arranged in the reaction chamber of the reactor (1), and the axis of each catalyst-coated body (13) is parallel to the axis of the reaction chamber.

5. The reactor according to claim 4, characterized in that The reactor (1) is provided with a raw material distributor (14), preferably the raw material distributor (14) is arranged at the top of the reaction chamber; and / or The catalyst coating body (13) is arranged in the reaction chamber so that the raw material contacts the non-coating part first and then contacts the coating part; and / or A plurality of catalyst coating body rings are arranged in the reaction chamber, the plurality of catalyst coating body rings are arranged at intervals along the radial direction of the reaction chamber, and each of the catalyst coating body rings comprises the catalyst coating body (13) arranged at intervals along the circumferential direction of the reaction chamber; and / or The feed port (11) and the discharge port (12) of the reactor (1) are respectively connected to the two ends of the reaction chamber. Preferably, the feed port (11) is connected to the top of the reaction chamber and communicates with the feed port of the raw material distributor (14).

6. The reactor according to claim 5, characterized in that The raw material distributor (14) is configured as a gas distributor, comprising a hemispherical distribution body connected to the feed port (11) of the reactor (1), wherein the hemispherical distribution body is provided with a plurality of distribution holes, and an impeller is installed in each of the distribution holes.

7. Use of the catalyst-coated body (13) according to any one of claims 1 to 3 and / or the reactor (1) according to any one of claims 4 to 6 in an endothermic reaction, preferably in a dehydrogenation reaction.

8. A method for dehydrogenating an organic hydride, characterized in that: The method uses the reactor (1) according to any one of claims 4 to 6, comprising coating a dehydrogenation catalyst on the catalyst coating body (13) and introducing an organic hydride into a reaction chamber.

9. The method according to claim 8, wherein: The organic hydride is fed into the reaction chamber through a raw material distributor (14); and / or The reaction conditions include: reaction pressure of 0-0.5 MPa, temperature of 220-380°C, mass space velocity of 0.1-10 h -1 ; and / or The organic hydride comprises at least one of methylcyclohexane, cyclohexane, tetralin, decalin, perhydroethylcarbazole and perhydrocarbazole; and / or The dehydrogenation catalyst comprises, by weight: 0.1% to 1% of active components, 0.3% to 2% of additives and 97% to 99.6% of carriers; Preferably, the active component comprises one or more of Pt, Pd, Rh, Ru and Au; and / or Preferably, the additive comprises one or more of chromium, molybdenum, tungsten, vanadium, niobium and tantalum; and / or Preferably, the carrier comprises one or more of alumina, zirconia and silica-alumina molecular sieve.

10. The method according to claim 8 or 9, wherein: The step of coating the dehydrogenation catalyst on the catalyst coating body (13) comprises: coating the coating slurry on the shell surface of the catalyst coating body (13), and then drying and calcining the slurry in sequence; Preferably, the coating is applied in the direction of feeding the organic hydride into the reactor (1); and / or Preferred drying conditions include: temperature 80-120°C, time 3-8h; and / or Preferred calcination conditions include: temperature 300-400°C, time 3-6h; and / or Preferably, the preparation of the coating slurry includes: adding deionized water to the dehydrogenation catalyst and stirring it thoroughly, adding a binder and a dispersant and ball milling them, and mixing them to form the coating slurry.

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