Organic liquid hydrogen release reaction system and method

Abstract

The application discloses an organic liquid hydrogen releasing reaction system and method. The system comprises a gas-liquid mixing chamber, a dehydrogenation reaction chamber and a catalytic combustion chamber, the catalytic combustion chamber and the dehydrogenation reaction chamber are arranged in a sleeve type structure from outside to inside, and the gas-liquid mixing chamber and the catalytic combustion chamber are communicated. The catalytic combustion chamber is provided with n catalyst beds, and each catalyst bed is filled with a mixture of a catalytic combustion catalyst and inert particles. The reaction system is used in the organic liquid hydrogen releasing reaction, and has the advantages of high dehydrogenation reaction conversion rate, low energy consumption of the reaction system, uniform temperature distribution of the reaction system and prolonged operation period of the device.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen storage, in particular to an organic liquid hydrogen release reaction system and method. BACKGROUND

[0002] Hydrogen produced from renewable energy is a potential alternative to conventional fossil energy carriers. In recent years, many renewable energy power generation devices have been built, especially photovoltaic power generation and wind power facilities. Due to the fluctuation of solar and wind energy production, they cannot provide reliable base load power. Therefore, large-scale energy storage is needed to compensate for seasonal imbalances.

[0003] Energy storage by liquid organic hydrogen carrier (LOHC) systems has received extensive attention. This technology makes it possible for liquid hydrogen storage to provide large-scale, long-duration energy storage without loss. In fact, the storage scale and time are only limited by the size of each tank and the technical availability of each LOHC compound. LOHC systems can achieve energy storage without binding or releasing CO2 or N2 from the atmosphere. Among different LOHC compounds, pure hydrocarbon systems have the advantages of low cost and complete compatibility with existing liquid fuel infrastructure, however, all pure hydrocarbon LOHC systems are characterized by relatively high dehydrogenation heat, so catalytic hydrogen release requires relatively high heat input, and the temperature is usually above 250℃. The most commonly used heat source is electric heating, however, there is also energy loss in the process of converting hydrogen energy into electrical energy, resulting in very low energy efficiency of the final energy storage system, so the reaction heat of the chemical reaction is a more ideal heat source.

[0004] CN112265961A discloses an online hydrogen supply system based on alcohol fuel reforming reaction, comprising a raw material tank, a heat exchanger connected with the raw material tank through a raw material metering pump, a hydrogen production-purification integrated reactor connected with the raw material tank through a fuel metering pump, an air pump connected to the hydrogen production-purification integrated reactor, a cooler, and a hydrogen storage tank connected to the cooler. The hydrogen production-purification integrated reactor comprises a vaporization chamber, a reforming reaction chamber, a catalytic combustion chamber, a hydrogen purification chamber, a temperature sensor, and a reforming product gas delivery coil. The reforming reaction chamber, the catalytic combustion chamber, and the hydrogen purification chamber are cylindrical sleeve structures arranged from outside to inside. The hydrogen supply system has the advantages of high hydrogen storage density, small volume weight, wide raw material sources, wide application range, and ready-to-use hydrogen.

[0005] CN112174089A discloses an organic liquid hydrogen supply system for a closed environment, comprising a storage unit, a hydrolysis hydrogen production unit, an organic liquid dehydrogenation unit and a product treatment unit, the hydrolysis hydrogen production unit uses metal hydride and water as raw materials to produce hydrogen and water vapor mixture, oxygen and mixed gas enter the organic liquid dehydrogenation unit to occur safe catalytic combustion reaction, organic liquid occurs catalytic dehydrogenation reaction at a certain temperature, and combustion tail gas water vapor is recycled after cooling in the product treatment unit. The system uses hydrogen and water vapor mixture as fuel, and water vapor as inert gas to reduce the hydrogen-oxygen reaction rate, ensure the safety of the system, has the advantages of no external heating, high hydrogen storage density, safety and reliability, no by-product gas emission, etc., and is suitable for closed environment, such as underwater vehicle, deep sea equipment, etc.

[0006] CN104888664A discloses a self-heating hydrogen supply device and its application. The self-heating hydrogen supply device adopts a concentric sleeve structure, comprising an inner tube (A) and an outer tube (B); the inner tube is a catalytic dehydrogenation reactor, and the outer tube is a hydrogen catalytic combustion reactor; the inner tube is filled with a whole hierarchical structure nanometer carbon fiber catalyst bed layer, and the outer wall of the inner tube is coated with a catalyst layer with a thickness of 0.15-2.5 μm for hydrogen catalytic combustion reaction; the inner diameter of the outer tube is 1.2-2 times the outer diameter of the inner tube.

[0007] The above method has achieved certain results in exploring organic liquid hydrogen supply device, but all have the problem of too concentrated catalytic combustion reaction leading to local high temperature of the reaction system and too large temperature difference of the dehydrogenation bed layer. Therefore, there is an urgent need to provide a new system suitable for organic liquid hydrogen release reaction. SUMMARY

[0008] The present application provides a new organic liquid hydrogen release reaction system and method to solve the problems of high energy consumption, high local temperature of the reaction system and large temperature difference of the dehydrogenation bed layer in the prior art.

[0009] The present application provides an organic liquid hydrogen release reaction system, wherein the organic liquid hydrogen release reaction system comprises a gas-liquid mixing chamber, a dehydrogenation reaction chamber and a catalytic combustion chamber, the catalytic combustion chamber and the dehydrogenation reaction chamber are arranged in a sleeve type structure from outside to inside, the gas-liquid mixing chamber and the catalytic combustion chamber are connected, the catalytic combustion chamber is provided with n catalyst bed layers, each catalyst bed layer is filled with a mixture of catalytic combustion catalyst and inert particles, and n is greater than or equal to 3, preferably n is 3-10, and more preferably n is 5-10.

[0010] Further, the sleeve structure is a cylindrical sleeve structure.

[0011] Further, the catalytic combustion catalyst in the catalytic combustion chamber is a supported particulate catalyst.

[0012] Further, in the catalytic combustion chamber, the volume ratio of the total loading amount V1 of the catalytic combustion catalyst to the total loading amount V2 of the inert particles is 0.3-1.0, preferably 0.4-0.8. Further, in the catalytic combustion chamber, the volume u of the mixture of the catalytic combustion catalyst and the inert particles loaded in each catalyst bed layer is a*(V1+V2) / n, wherein n is the number of catalyst bed layers, and a is 0.8-1.2.

[0013] Further, in the catalytic combustion chamber, the total loading amount of the catalytic combustion catalyst is V1, and the volume v of the catalytic combustion catalyst loaded in each catalyst bed layer is c*V1 / n, wherein n is the number of catalyst bed layers, and c is 0.1-2.0, preferably 0.3-1.8.

[0014] Further, the volume of the catalytic combustion catalyst loaded in each catalyst bed layer shows an overall increasing trend in the order of catalyst loading (i.e. from bottom to top), i.e. the c values of two adjacent catalyst bed layers can be equal or differ by at most 0.5.

[0015] Further, the inert particles are ceramic particles, and preferably, the inert particles have the same size as the catalyst particles.

[0016] Further, the catalytic combustion catalyst provided in the catalytic combustion chamber comprises, in parts by weight: (a) 0.01-5 parts of one or more elements selected from Group VIII of the Periodic Table of Elements, (b) 95-99.99 parts of a carrier; the Group VIII element is at least one of Pt, Pd, Rh or Ir; and the carrier is one or more of alumina or silicate ceramic, preferably alumina.

[0017] Further, the catalytic combustion catalyst can be prepared by an equal-volume impregnation method.

[0018] Further, the dehydrogenation reaction chamber is loaded with a dehydrogenation catalyst, and the dehydrogenation catalyst is a supported particulate catalyst.

[0019] Further, the dehydrogenation catalyst arranged in the dehydrogenation reaction chamber comprises, in parts by weight, (a) 0.1-5 parts of one or more of elements selected from Group VIII of the Periodic Table of Elements, (b) 95-99.9 parts of a carrier; the element of Group VIII is at least one of Pt, Pd, Rh or Ir, and the carrier is a carbon carrier. The carbon carrier is one or more of carbon nanotubes, graphene or graphyne, and is preferably carbon nanotubes. Further, the carbon carrier used by the dehydrogenation catalyst can also be a halogen-modified carbon carrier, wherein the halogen is at least one of fluorine, chlorine, bromine or iodine, and the halogen accounts for 0.1%-5.0% of the mass of the halogen-modified carbon carrier.

[0020] Further, the dehydrogenation catalyst is prepared by an equal-volume impregnation method.

[0021] Further, the total height of the catalyst bed arranged in the catalytic combustion chamber is 1.0-2.0 times, and preferably 1.0-1.5 times, the total height of the catalyst bed arranged in the dehydrogenation reaction chamber.

[0022] The second aspect of the present application provides an organic liquid hydrogen release reaction method, wherein the above-mentioned organic liquid hydrogen release reaction system is used.

[0023] Further, the organic liquid hydrogen release reaction method comprises: the hydrogen-rich organic liquid enters the dehydrogenation reaction chamber to contact the dehydrogenation catalyst to perform a dehydrogenation reaction, the dehydrogenated organic liquid enters the gas-liquid mixing chamber, and then enters the catalytic fuel chamber to contact the catalytic combustion catalyst to perform a reaction, and the obtained reaction product is discharged from the reaction system.

[0024] Further, the hydrogen-rich organic liquid is selected from one or more of cyclohexane, methylcyclohexane, tetrahydronaphthalene, decahydronaphthalene, perhydroazepine, perhydrophenanthrene, perhydroanthracene, perhydrocarbazole or derivatives thereof, components cut from petroleum or fractionated oil of petroleum, and materials after hydrogenation of the cut components, and is preferably at least one of cyclohexane, methylcyclohexane and perhydrocarbazole.

[0025] Further, the dehydrogenated organic liquid is selected from at least one of the corresponding organic substances after dehydrogenation of the hydrogen-rich organic liquid.

[0026] Further, the maximum axial temperature difference in the catalytic combustion chamber is 20-100℃.

[0027] Further, the maximum axial temperature difference in the dehydrogenation reaction chamber is 10-40℃.

[0028] Further, the reaction conditions for the catalytic combustion reaction in the catalytic combustion chamber are as follows: the reaction pressure is 0.1-1.0 MPa, the reaction temperature is 500-650℃, the volume reaction space velocity is 5000-50000 h-1, and the reaction time is 0.1-1.0 s. -1.

[0029] Further, the reaction conditions for the dehydrogenation reaction in the dehydrogenation reaction chamber are as follows: the reaction pressure is 0.1-1.0 MPa, the reaction temperature is 270-380℃, the mass reaction space velocity is 1-20 h -1 .

[0030] In the present application, the catalytic combustion chamber supplies heat for the dehydrogenation reaction chamber.

[0031] Compared with the prior art, the present application has the following advantages:

[0032] The organic liquid hydrogen releasing reaction system provided by the present application sets the catalytic combustion chamber and the dehydrogenation reaction chamber in a sleeve type structure, and sets multiple catalyst bed layers in the catalytic combustion chamber, each of which is filled with catalytic combustion catalyst and inert particles. In this way, the internal temperature difference of the two reaction chambers can be effectively controlled, and the catalytic combustion chamber can supply heat for the dehydrogenation reaction chamber. Under the condition that the catalytic combustion reaction is fully converted (the conversion rate can be more than 99%), the dehydrogenation reaction conversion rate can be more than 80%, even 95.6%. Moreover, the organic liquid hydrogen releasing reaction system of the present application is also conducive to the long-period stable operation of the reaction. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1 Fig. 1 is a structural schematic diagram of the organic liquid hydrogen releasing reaction system of the present application;

[0034] In the drawings, the reference signs are explained as follows:

[0035] 1-gas-liquid mixing chamber, 2-dehydrogenation reaction chamber, 3-catalytic combustion chamber. DETAILED DESCRIPTION

[0036] The technical solutions of the present application are further described below in combination with the specific embodiments.

[0037] Example 1

[0038] Take 40 ml dehydrogenation catalyst, 54 ml catalytic combustion catalyst, dehydrogenation catalyst is Pt / CNT, the mass content of Pt is 1%, catalytic combustion catalyst is Pd / Al2O3, the mass content of Pd is 0.4%. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The ratio of the total height of the catalyst bed provided by the catalytic combustion chamber to the total height of the catalyst bed provided by the dehydrogenation reaction chamber is 1.2, and the bottoms of the two catalyst loading sections are flush. The bottom of the catalytic combustion catalyst loading section is loaded in the axial direction in the order of 6 layers (4.5 ml catalyst-19.5 ml porcelain ball), (6 ml catalyst-18 ml porcelain ball), (9 ml catalyst-15 ml porcelain ball), (9 ml catalyst-15 ml porcelain ball), (12 ml catalyst-12 ml porcelain ball), and (13.5 ml catalyst-12 ml porcelain ball). The particle sizes of the porcelain balls and the catalysts are the same, and the catalyst and the porcelain balls in each layer are uniformly mixed. After the catalyst is loaded, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0039] An appropriate amount of benzene is delivered to the gas-liquid mixing chamber, and an appropriate amount of cyclohexane is delivered to the dehydrogenation reaction chamber. After the benzene and the appropriate amount of air are mixed uniformly in the gas-liquid mixing chamber, they enter the catalytic combustion chamber for catalytic combustion reaction. The reaction conditions of the catalytic combustion reaction are as follows: the reaction pressure is 0.1 MPa, the volume reaction space velocity is 20000 h -1 , and the reaction conditions of the dehydrogenation reaction are as follows: the reaction pressure is 0.1 MPa, the mass reaction space velocity is 6 h -1 In the present application, the catalytic combustion chamber provides heat for the dehydrogenation reaction chamber. The highest temperature and the lowest temperature of each bed layer are measured by K-type thermocouples embedded in the dehydrogenation reaction bed layer and the catalytic combustion bed layer. The dehydrogenation reaction conversion rate is measured by gas chromatography, and the results are shown in Table 1.

[0040] Example 2

[0041] Take 40 ml dehydrogenation catalyst, 45 ml catalytic combustion catalyst, dehydrogenation catalyst is Pt / CNT, the mass content of Pt is 1%, catalytic combustion catalyst is Pd / Al2O3, the mass content of Pd is 0.4%. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The total height of the catalyst bed provided by the catalytic combustion chamber is equal to the total height of the catalyst bed provided by the dehydrogenation reaction chamber, and the bottoms of the two catalyst loading sections are flush. The bottom of the catalytic combustion catalyst loading section is loaded in three layers along the axial direction (10 ml catalyst-30 ml porcelain ball), (15 ml catalyst-25 ml porcelain ball), and (20 ml catalyst-20 ml porcelain ball). The particle size of the porcelain ball and the catalyst is the same, and the catalyst and the porcelain ball in each layer are uniformly mixed. After the catalyst is loaded, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0042] The benzene is transported to the gas-liquid mixing chamber, and the cyclohexane is transported to the dehydrogenation reaction chamber. After the benzene and air are uniformly mixed in the gas-liquid mixing chamber, they enter the catalytic combustion chamber for catalytic combustion reaction. The flow rates of the cyclohexane and air are the same as in Example 1. The highest and lowest temperatures of the respective bed layers are measured by K-type thermocouples embedded in the dehydrogenation reaction bed layer and the catalytic combustion bed layer. The dehydrogenation reaction conversion rate is measured by gas chromatography, and the results are shown in Table 1.

[0043] Example 3

[0044] Take 40 ml dehydrogenation catalyst, 45 ml catalytic combustion catalyst, dehydrogenation catalyst is Pt / CNT, the mass content of Pt is 1%, catalytic combustion catalyst is Pd / Al2O3, the mass content of Pd is 0.4%. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The total height of the catalyst bed provided by the catalytic combustion chamber is equal to the total height of the catalyst bed provided by the dehydrogenation reaction chamber, and the bottoms of the two catalyst loading sections are flush. The bottom of the catalytic combustion catalyst loading section is loaded in three layers along the axial direction (10 ml catalyst-30 ml porcelain ball), (15 ml catalyst-25 ml porcelain ball), and (20 ml catalyst-20 ml porcelain ball). The particle size of the porcelain ball and the catalyst is the same, and the catalyst and the porcelain ball in each layer are uniformly mixed. After the catalyst is loaded, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0045] The benzene is transported to the gas-liquid mixing chamber, and the cyclohexane is transported to the dehydrogenation reaction chamber. After the benzene and air are uniformly mixed in the gas-liquid mixing chamber, they enter the catalytic combustion chamber for catalytic combustion reaction. The flow rates of the cyclohexane and air are the same as in Example 1. The highest and lowest temperatures of the respective bed layers are measured by K-type thermocouples embedded in the dehydrogenation reaction bed layer and the catalytic combustion bed layer. The dehydrogenation reaction conversion rate is measured by gas chromatography, and the results are shown in Table 1.

[0046] Example 4

[0047] Take 40 ml of dehydrogenation catalyst, 37 ml of catalytic combustion catalyst, the dehydrogenation catalyst is Pt / CNT, the mass content of Pt is 1%, the catalytic combustion catalyst is Pd / Al2O3, the mass content of Pd is 0.4%. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The total height of the catalyst bed provided by the catalytic combustion chamber is equal to the total height of the catalyst bed provided by the dehydrogenation reaction chamber, and the bottoms of the two catalyst loading sections are flush. The bottom of the catalytic combustion catalyst loading section is loaded in 6 layers along the axial direction in order (2 ml of catalyst-18 ml of porcelain ball), (4 ml of catalyst-16 ml of porcelain ball), (6 ml of catalyst-14 ml of porcelain ball), (6 ml of catalyst-14 ml of porcelain ball), (9 ml of catalyst-11 ml of porcelain ball), and (10 ml of catalyst-12 ml of porcelain ball). The particle sizes of the porcelain balls and the catalysts are the same, and each layer of catalyst and porcelain ball is uniformly mixed. After the catalyst is loaded, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0048] The benzene is transported to the gas-liquid mixing chamber, and the cyclohexane is transported to the dehydrogenation reaction chamber. After the benzene and air are uniformly mixed in the gas-liquid mixing chamber, they enter the catalytic combustion chamber for catalytic combustion reaction. The flow rates of the cyclohexane and air are the same as in Example 1. The highest and lowest temperatures of the respective beds are measured by K-type thermocouples embedded in the dehydrogenation reaction bed and the catalytic combustion bed. The dehydrogenation reaction conversion rate is measured by gas chromatography. The results are shown in Table 1.

[0049] Example 5

[0050] Take 40 ml of dehydrogenation catalyst, 54 ml of catalytic combustion catalyst, the dehydrogenation catalyst is Pt / CNT, the mass content of Pt is 1%, the catalytic combustion catalyst is Pd / Al2O3, the mass content of Pd is 0.4%. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The total height of the catalyst bed provided by the catalytic combustion chamber is equal to the total height of the catalyst bed provided by the dehydrogenation reaction chamber, and the bottoms of the two catalyst loading sections are flush. The bottom of the catalytic combustion catalyst loading section is loaded in 6 layers along the axial direction in order (2 ml of catalyst-18 ml of porcelain ball), (4 ml of catalyst-16 ml of porcelain ball), (6 ml of catalyst-14 ml of porcelain ball), (6 ml of catalyst-14 ml of porcelain ball), (9 ml of catalyst-11 ml of porcelain ball), and (10 ml of catalyst-12 ml of porcelain ball). The particle sizes of the porcelain balls and the catalysts are the same, and each layer of catalyst and porcelain ball is uniformly mixed. After the catalyst is loaded, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0051] The appropriate amount of benzene is delivered to the gas-liquid mixing chamber, and the appropriate amount of cyclohexane is delivered to the dehydrogenation reaction chamber. The benzene and the appropriate amount of air are mixed uniformly in the gas-liquid mixing chamber and then enter the catalytic combustion chamber to perform the catalytic combustion reaction. The reaction conditions of the catalytic combustion reaction are as follows: the reaction pressure is 0.1 MPa, the volume reaction space velocity is 30000 h -1 , and the reaction conditions of the dehydrogenation reaction are as follows: the reaction pressure is 0.1 MPa, the mass reaction space velocity is 6 h -1 In the present application, the catalytic combustion chamber supplies heat to the dehydrogenation reaction chamber. The highest temperature and the lowest temperature of the respective bed layers are measured by the K-type thermocouples embedded in the dehydrogenation reaction bed layer and the catalytic combustion bed layer. The dehydrogenation reaction conversion rate is measured by gas chromatography, and the results are shown in Table 1.

[0052] Comparative Example 1

[0053] 40 ml of the dehydrogenation catalyst and 45 ml of the catalytic combustion catalyst are taken. The dehydrogenation catalyst is Pt / CNT, and the mass content of Pt is 1%. The catalytic combustion catalyst is Pd / Al2O3, and the mass content of Pd is 0.4%. The total height of the catalyst bed layer arranged in the catalytic combustion chamber is equal to the total height of the catalyst bed layer arranged in the dehydrogenation reaction chamber. The dehydrogenation catalyst is loaded into the dehydrogenation reaction chamber, and the catalytic combustion catalyst is loaded into the catalytic combustion chamber. The two kinds of catalysts are uniformly loaded respectively. After the loading of the catalysts is completed, the catalytic combustion chamber and the dehydrogenation reaction chamber are sealed.

[0054] The benzene is delivered to the gas-liquid mixing chamber, and the cyclohexane is delivered to the dehydrogenation reaction chamber. The benzene and the air are mixed uniformly in the gas-liquid mixing chamber and then enter the catalytic combustion chamber to perform the catalytic combustion reaction. The flow rates of the cyclohexane and the air are the same as those in Example 2. The highest temperature and the lowest temperature of the respective bed layers are measured by the K-type thermocouples embedded in the dehydrogenation reaction bed layer and the catalytic combustion bed layer. The dehydrogenation reaction conversion rate is measured by gas chromatography, and the results are shown in Table 1.

[0055] Table 1

[0056]

[0057] Note: In each of the examples and the comparative examples, the conversion rate of the catalytic combustion reaction is more than 99%.

[0058] The examples described in the present application are only detailed descriptions of the technical solutions of the present application, but the present application is not limited to the above examples. That is, the present application can be implemented without relying on the steps described in the above examples. In summary, any improvement on the present application made by a person skilled in the art, including the replacement of the raw materials and additives described in the present application, the selection of the specific implementation modes, etc., all belong to the protection scope and the disclosure scope of the present application.

Claims

1. An organic liquid hydrogen release reaction system, wherein, The organic liquid hydrogen release reaction system includes a gas-liquid mixing chamber, a dehydrogenation reaction chamber, and a catalytic combustion chamber. The catalytic combustion chamber and the dehydrogenation reaction chamber are arranged in a sleeve-like structure from the outside to the inside. The gas-liquid mixing chamber and the catalytic combustion chamber are connected. The catalytic combustion chamber is provided with n catalyst beds. Each catalyst bed is filled with a mixture of catalytic combustion catalyst and inert particles, where n is 3 or more. In the catalytic combustion chamber, the volume of the mixture of catalytic combustion catalyst and inert particles packed in each catalyst bed is u = a * (V1 + V2) / n, where n is the number of catalyst beds and a takes a value of 0.8-1.2; the total amount of catalytic combustion catalyst packed is V1, and the volume of catalytic combustion catalyst packed in each catalyst bed is v = c * V1 / n, where n is the number of catalyst beds and c takes a value of 0.1-2.0; The volume of catalytic combustion catalyst packed in each catalyst bed generally increases according to the order of catalyst loading, that is, the c value of two adjacent catalyst beds is equal or differs by a maximum of 0.

5.

2. The system according to claim 1, characterized in that, In the catalytic combustion chamber, the volume ratio of the total catalytic combustion catalyst loading V1 to the total inert particle loading V2 is 0.3-1.

0.

3. The system according to claim 2, characterized in that, In the catalytic combustion chamber, the volume ratio of the total catalytic combustion catalyst loading V1 to the total inert particle loading V2 is 0.4-0.

8.

4. The system according to claim 1, characterized in that, The catalytic combustion chamber is equipped with n catalyst beds, each catalyst bed being filled with a mixture of catalytic combustion catalyst and inert particles, where n takes the value of 3-10.

5. The system according to claim 4, characterized in that, The catalytic combustion chamber is equipped with n catalyst beds, each catalyst bed being filled with a mixture of catalytic combustion catalyst and inert particles, where n takes the value of 5-10.

6. The system according to claim 1 or 2, characterized in that, In the catalytic combustion chamber, the total amount of catalytic combustion catalyst is V1, and the volume of catalytic combustion catalyst in each catalyst bed is v=c*V1 / n, where n is the number of catalyst beds and c is 0.3-1.

8.

7. The system according to claim 1, characterized in that, The catalytic combustion catalyst disposed in the catalytic combustion chamber comprises, by weight, (a) 0.01-5 parts selected from one or more elements of Group VIII of the periodic table, and (b) 95-99.99 parts of a support; wherein the Group VIII element is at least one of Pt, Pd, Rh or Ir; and the support is one or more of alumina or silicate ceramics. And / or, the dehydrogenation catalyst disposed in the dehydrogenation reaction chamber comprises, by weight, (a) 0.1-5 parts selected from one or more elements selected from Group VIII of the periodic table, and (b) 95-99.9 parts of a support; wherein the Group VIII element is at least one of Pt, Pd, Rh or Ir, and the support is a carbon support; wherein the carbon support is one or more of carbon nanotubes, graphene or graphyne. And / or, the inert particles are ceramic particles.

8. The system according to claim 7, characterized in that, The support for the catalytic combustion catalyst is alumina; And / or, the support for the dehydrogenation catalyst is carbon nanotubes; And / or, the size of the inert particles is the same as that of the catalytic combustion catalyst particles.

9. The system according to claim 1, characterized in that, The total height of the catalyst bed in the catalytic combustion chamber is 1.0-2.0 times the total height of the catalyst bed in the dehydrogenation reaction chamber.

10. The system according to claim 9, characterized in that, The total height of the catalyst bed in the catalytic combustion chamber is 1.0-1.5 times the total height of the catalyst bed in the dehydrogenation reaction chamber.

11. A method for hydrogen release reaction of an organic liquid, characterized in that, The organic liquid hydrogen release reaction system according to any one of claims 1-10.

12. The method according to claim 11, characterized in that, The organic liquid hydrogen release reaction method includes: a hydrogen-rich organic liquid entering a dehydrogenation reaction chamber and contacting a dehydrogenation catalyst to carry out a dehydrogenation reaction; the dehydrogenated organic liquid entering a gas-liquid mixing chamber and then entering a catalytic fuel chamber to contact a catalytic combustion catalyst to carry out a reaction; and the resulting reaction products being discharged from the reaction system respectively.

13. The method according to claim 12, characterized in that, The hydrogen-rich organic liquid is selected from one or more of cyclohexane, methylcyclohexane, tetrahydronaphthalene, decahydronaphthalene, perhydronitroethylcarbazole, perhydrophenanthrene, perhydroanthracene, perhydrocarbazole or their derivatives; the dehydrogenated organic liquid is selected from at least one of the organic compounds corresponding to the dehydrogenated hydrogen-rich organic liquid.

14. The method according to claim 13, characterized in that, The hydrogen-rich organic liquid is at least one of cyclohexane, methylcyclohexane, and perhydrocarbazole.

15. The method according to any one of claims 12-14, characterized in that, The catalytic combustion chamber supplies heat to the dehydrogenation reaction chamber; and / or, the maximum axial temperature difference in the catalytic combustion chamber is 20-100℃; the maximum axial temperature difference in the dehydrogenation reaction chamber is 10-40℃.

16. The method according to any one of claims 12-14, characterized in that, The reaction conditions for the catalytic combustion reaction in the catalytic combustion chamber are as follows: reaction pressure 0.1 MPa-1.0 MPa, reaction temperature 500-650℃, and volumetric space velocity 5000-50000 h⁻¹. -1 ; and / or, the reaction conditions for the dehydrogenation reaction in the dehydrogenation reaction chamber are as follows: reaction pressure of 0.1 MPa-1.0 MPa, reaction temperature of 270-380 °C, and mass space velocity of 1-20 h⁻¹. -1 .

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