Dehydrogenation system

Abstract

To provide a dehydrogenation system which can efficiently utilize heat of an external heat source.SOLUTION: A dehydrogenation system has a preliminary reactor, a main reactor, a heating section, and a heat recovery section. The preliminary reactor is configured to produce hydrogen from a vaporized hydrogenated aromatic compound. The main reactor is configured to produce hydrogen from the hydrogenated aromatic compound which has passed through the preliminary reactor. The heating section is configured to supply heat to the main reactor. The heat recovery section is configured to recover heat from an external heat source and supply the recovered heat to the preliminary reactor.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a dehydrogenation reaction system configured to produce hydrogen from hydrogenated aromatic compounds. [Background technology]

[0002] One method for storing and transporting hydrogen is the organic chemical hydride method, in which aromatic compounds such as toluene are hydrogenated and stored or transported in the form of hydrogenated aromatic compounds (organic hydrides).The dehydrogenation reaction of hydrogenated aromatic compounds is an endothermic reaction, so heat must be added from an external source.

[0003] Patent Document 1 discloses that the heat generated in a synthetic natural gas generator is received as an external heat source, and this heat is utilized to carry out a dehydrogenation reaction. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Patent No. 6194143 Summary of the Invention [Problem to be solved by the invention]

[0005] However, in dehydrogenation reaction systems, the majority of heat that can be recovered from external heat sources is generally in the temperature range of 300°C or less. Therefore, it is often difficult to apply the heat recovered from external heat sources to the dehydrogenation process in a high-temperature range, and the types of external heat sources that can be used are limited. Another inconvenience is that the heat exchange medium recovered from the external heat source must be reheated to the temperature required for the high-temperature dehydrogenation process.

[0006] The present invention has been made in view of the above circumstances, and provides a dehydrogenation reaction system that can efficiently utilize heat from an external heat source. [Means for solving the problem]

[0007] According to the present invention, the following inventions are provided. [1] A dehydrogenation reaction system having a preliminary reactor, a main reactor, a heating section, and a heat recovery section, the pre-reactor is configured to produce hydrogen from the vaporized hydrogenated aromatic compound; the reactor is configured to produce hydrogen from the hydrogenated aromatic compounds that have passed through the pre-reactor; the heating section is configured to supply heat to the reactor; The dehydrogenation reaction system, wherein the heat recovery unit is configured to recover heat from an external heat source and supply the recovered heat to the pre-reactor. [2] The dehydrogenation reaction system according to [1], A dehydrogenation reaction system, wherein the heat recovery unit is configured to recover heat in a temperature range of 250°C to 500°C. [3] The dehydrogenation reaction system according to [1] or [2], a dehydrogenation reaction system, wherein the pre-reactor is a multi-tube reactor having a cylindrical shell and a plurality of tubes extending within the shell; [4] A dehydrogenation reaction system according to any one of [1] to [3], The dehydrogenation reaction system, wherein the heat recovery section is configured to supply heat from the external heat source to the pre-reactor via hot oil. [5] A dehydrogenation reaction system according to any one of [1] to [4], The dehydrogenation reaction system is configured so that the heat recovery unit also supplies heat to other heat demand units other than the main reactor. [6] A dehydrogenation reaction system according to any one of [1] to [5], a dehydrogenation reaction system, wherein the external heat source is heat generated by an exothermic reaction in a methanation reaction section; [7] [6] The dehydrogenation reaction system according to [6], The methanation reaction section comprises a multi-tubular reactor having a cylindrical shell and a plurality of tubes extending within the shell. [Effects of the Invention]

[0008] The dehydrogenation reaction system of the present invention makes it possible to effectively utilize heat from an external heat source. [Brief explanation of the drawings]

[0009] [Figure 1] 1 is a diagram showing a schematic configuration of a dehydrogenation reaction system 1. FIG. [Figure 2] FIG. 1 is a diagram showing a schematic configuration of a dehydrogenation reaction system 1A. [Figure 3] 1 is a diagram showing a schematic configuration of a variation of the dehydrogenation reaction section 13 and the heat recovery section 16. FIG. DETAILED DESCRIPTION OF THE INVENTION

[0010] The following describes embodiments of the present invention. The various features shown in the following embodiments can be combined with each other. Furthermore, each feature can be an invention independently.

[0011] 1. First embodiment As shown in FIG. 1, the dehydrogenation reaction system 1 includes an evaporator 11, a superheater 12, a dehydrogenation reaction section 13, a separator 14, a heating furnace 15, and a heat recovery section 16. The dehydrogenation reaction system 1 is connected to a tank 4A via a flow path. The tank 4A contains a hydrogenated aromatic compound (liquid) as a raw material. The hydrogenated aromatic compound (liquid) is supplied into the dehydrogenation reaction system 1 by a pump 4B. Although the drawing shows the process fluid flowing from top to bottom, the process fluid may flow either downward or upward.

[0012] The evaporator 11 is configured to vaporize the supplied hydrogenated aromatic compound (liquid). The superheater 12 is configured to further heat the hydrogenated aromatic compound vaporized in the evaporator 11 to increase its temperature. In this embodiment, the evaporator 11 and the superheater 12 utilize heat from the heat recovery section 16, but this is not limiting. For example, the heat discharged from the dehydrogenation reaction system 1 or excess heat from the heating furnace 15 may be utilized.

[0013] The dehydrogenation reaction section 13 includes a preliminary reactor 13A and a main reactor 13B. Here, an example is shown in which one preliminary reactor 13A is arranged upstream of the main reactor 13B, but multiple preliminary reactors 13A may be arranged upstream of the main reactor 13B. Regardless of the number of preliminary reactors 13A arranged, the final conversion rate of the organic hydride in the dehydrogenation reaction system 1 is determined by the environment of the main reactor 13B (reaction temperature, catalyst amount, etc.).

[0014] The preliminary reactor 13A is configured to produce hydrogen from the vaporized hydrogenated aromatic compound. The main reactor 13B is configured to produce hydrogen from the hydrogenated aromatic compound that has passed through the preliminary reactor 13A. In this embodiment, the hydrogenated aromatic compound is methylcyclohexane (MCH). The preliminary reactor 13A and the main reactor 13B may be configured, for example, as a shell-and-tube multi-tube reactor. The preliminary reactor 13A and the main reactor 13B each have a cylindrical shell and a plurality of tubes extending within the shell. The inner space of each tube is isolated from the inner space of the shell. The inside of each tube is filled with a dehydrogenation catalyst that promotes the dehydrogenation reaction.

[0015] The dehydrogenation catalyst used in the preliminary reactor 13A and the main reactor 13B may be a catalyst in which at least one active metal selected from nickel (Ni), platinum (Pt), palladium (Pd), rhodium (Rh), iridium (Ir), and ruthenium (Ru) is supported on a carrier selected from alumina, silica alumina, and silica. However, the type of catalyst is not limited to these, and any known catalyst used in the dehydrogenation reaction of organic hydrides may be used.

[0016] The same catalyst may be used in the preliminary reactor 13A and the main reactor 13B, or different catalysts may be used in each. The amount (weight) of catalyst provided in the preliminary reactor 13A and the main reactor 13B may be determined depending on the reaction rate expected in the preliminary reactor 13A and the main reactor 13B. For example, if the reaction rate in the preliminary reactor 13A is expected to be 30 to 40%, i.e., the conversion rate of the organic hydride is expected to be 30 to 40%, the ratio (weight) of the amount of catalyst provided in the preliminary reactor 13A and the main reactor 13B may be set to about 30:70 to 40:60.

[0017] The organic hydride that is the reactant of the dehydrogenation reaction in the dehydrogenation reaction system 1 is not limited to MCH, but may be a monocyclic hydrogenated aromatic compound such as cyclohexane, a bicyclic hydrogenated aromatic compound such as tetralin, decalin, or methyldecalin, or a tricyclic hydrogenated aromatic compound such as tetradecahydroanthracene, either alone or as a mixture of two or more of them. Taking into consideration the convenience of storage and transportation, it is advisable to select an organic hydride that can be handled as a stable liquid at room temperature and normal pressure.

[0018] Furthermore, the aromatic compounds generated together with hydrogen in the dehydrogenation reaction of the dehydrogenation reaction system 1 are not limited to toluene, and depending on the type of organic hydride described above, for example, monocyclic aromatic compounds such as benzene and xylene, bicyclic aromatic compounds such as naphthalene, tetralin and methylnaphthalene, and tricyclic aromatic compounds such as anthracene can be used alone or as a mixture of two or more types.

[0019] Separator 14 is configured to separate the product gas containing hydrogen from the liquefied toluene by cooling the reaction product. A known adsorption device (not shown) capable of removing toluene and unreacted MCH vapor components contained in the product gas may be disposed downstream of separator 14. The separated toluene is sent to a storage device or the like and stored therein, and can then be circulated to the hydrogenation system by, for example, a known transportation means (pipeline, vehicle, ship, etc.). The separated toluene can also be used for other purposes, such as blending with gasoline.

[0020] The heating furnace 15 corresponds to the heating section of the present invention and is configured to supply heat to the reactor 13B. The heating furnace 15 can be configured to obtain the desired amount of heat by burning natural gas, for example. However, other known configurations, such as a configuration using an electric heating wire, can be used as long as the desired amount of heat can be obtained stably. The heating furnace 15 heats the thermal oil (hot oil) in the furnace to about 400°C. The heated thermal oil is transported to the reactor 13B, and the thermal oil heats the hydrogenated aromatic compound and catalyst in the tubes of the reactor 13B.

[0021] The heat exchange medium is preferably a thermal oil capable of transferring high-temperature heat at normal pressure, but other heat exchange media such as high-pressure steam or gas at about 400°C can also be used. A suitable example of the heat exchange medium is a mixture of diphenyl oxide and biphenyl. However, other types of heat exchange oils may also be used as long as they have good chemical stability under the temperature conditions used as a heat source for the dehydrogenation reaction.

[0022] The heat recovery section 16 is configured to recover heat from an external heat source and supply the recovered heat to the pre-reactor 13A. In this embodiment, the heat recovery section 16 is configured to receive heat from the methanation reactor 2. The heat recovery section 16 recovers the heat generated by the methanation reaction in the methanation reactor 2 by heat exchange with heat transfer oil. The heat transfer oil heated in the methanation reactor 2 is transported into the shell of the pre-reactor 13A. This heats the hydrogenated aromatic compound and catalyst in the tubes of the pre-reactor 13A.

[0023] The heat recovery section 16 is configured to recover heat in the temperature range of 250°C to 500°C, and is typically configured to circulate a thermal oil at approximately 300°C. The temperature of the circulated thermal oil is preferably approximately 280°C to 350°C, and more preferably approximately 300°C to 320°C. This is because a thermal oil temperature below 280°C reduces the MCH conversion rate in the dehydrogenation reaction, while a thermal oil temperature above 350°C reduces the effect of suppressing temperature rise in the methanation reaction. As with the heating furnace 15, the heat exchange medium is preferably a thermal oil capable of transferring high-temperature heat at normal pressure, but other heat exchange media such as high-pressure steam or gas at approximately 300°C can also be used.

[0024] Here, we will explain the schematic configuration of the methanation reactor 2, which is an example of an external heat source from which the heat recovery unit 16 receives heat. The methanation reactor 2 includes an input unit 21, a methanation reactor 22, a first separator 23, and a second separator 24.

[0025] The input unit 21 is configured to receive carbon dioxide and hydrogen as raw materials. The carbon dioxide used may be carbon dioxide in the air or carbon dioxide in exhaust gas generated by fuel combustion in a generator, internal combustion engine, etc. The hydrogen used may be hydrogen supplied from an external source or hydrogen generated in the dehydrogenation reaction system 1.

[0026] The methanation reactor 22 corresponds to the methanation reaction section of the present invention and is configured to use hydrogen and carbon dioxide as raw materials and produce methane and water by the Sabatier reaction in the presence of a catalyst. A nickel-based catalyst is used as the catalyst. In this embodiment, the methanation reactor 22 is configured as a shell-and-tube multi-tubular reactor. For convenience of explanation, an example in which a single reactor is arranged is shown here, but the present invention can also be suitably applied to a system in which multiple methanation reactors 22 are arranged. Because the methanation reaction is an exothermic reaction, the heat transfer oil in the cylindrical shell is heated to approximately 300°C by the heat generated in the multiple tubes of the methanation reactor 22. This heated heat transfer oil is sent to the preliminary reactor 13A by the heat recovery section 16 described above. When the methanation reactor 22 is a heat exchanger-type reactor as in this embodiment, heat recovery is performed directly by passing the heat transfer oil through the methanation reactor 22. However, the heat recovery method using the heat recovery section 16 is not limited to this.

[0027] In the first separator 23, the product gas containing gaseous methane and hydrogen is separated from liquid water, and the product gas is sent to the second separator 24. The second separator 24 separates methane from the product gas. The second separator 24 is a known device that uses, for example, pressure swing adsorption (PSA) or a hydrogen separation membrane, and separates hydrogen and methane from the product gas containing methane and hydrogen.

[0028] Although the methanation reactor 2 is a suitable example of a heat source for the dehydrogenation reaction system 1, the external heat source is not necessarily limited to the methanation reactor 2. A fuel cell that operates at high temperatures (e.g., 600°C to 1000°C), such as a solid oxide fuel cell (SOFC), can also be used as the external heat source. Furthermore, the reaction heat of a carbon dioxide capture and utilization (CCU) process, which converts CO2 and water into methanol and oxygen at high temperatures (e.g., 600°C to 850°C), can also be used as the external heat source.

[0029] The dehydrogenation reaction system 1 receives heat generated in the methanation reactor 22 via the heat recovery section 16 and uses this heat to perform a dehydrogenation reaction in the preliminary reactor 13A. The heat recovered by the heat recovery section 16 is supplied to the preliminary reactor 13A, which plays a supporting role, rather than to the main reactor 13B, which determines the final conversion rate of the organic hydride. Therefore, even if the heat recovery section 16 can only recover heat in the temperature range of approximately 250°C to 350°C, the final conversion rate of the organic hydride is hardly affected, even without the need for a separate heating means for reheating. Therefore, heat in the temperature range of approximately 250°C to 350°C, which is relatively easy to obtain, can be effectively utilized in the preliminary reactor 13A. By utilizing the heat recovered by the heat recovery section 16 in heat demand sections such as the preliminary reactor 13A, the heat required by the main reactor 13B (heat duty) is significantly reduced, thereby reducing the amount of heat input to the heating furnace 15. In other words, it can be said that the dehydrogenation reaction system 1 achieves optimal overall heat utilization.

[0030] As described above, in the preliminary reactor 13A, hydrogen and toluene are produced by the dehydrogenation reaction of MCH in the presence of a dehydrogenation catalyst. The preliminary reactor 13A is an auxiliary reactor for the subsequent main reactor 13B. The product from the preliminary reactor 13A becomes the reactant supplied to the main reactor 13B, and by appropriately controlling the amount of catalyst placed in the preliminary reactor 13A and the reaction temperature, it is possible to adjust the hydrogen concentration (MCH conversion rate or reaction rate) of the reactant supplied to the main reactor 13B within an appropriate range.

[0031] The amount of hydrogen generated by the dehydrogenation reaction in the preliminary reactor 13A is set to be less than the amount of hydrogen generated by the dehydrogenation reaction in the main reactor 13B. The product of the preliminary reactor 13A (containing a predetermined concentration of hydrogen and unreacted MCH) is sent to the main reactor 13B.

[0032] In the main reactor 13B, hydrogen and toluene are produced by a dehydrogenation reaction of MCH (MCH that was unreacted in the preliminary reactor 13A) in the presence of a dehydrogenation catalyst. In the main reactor 13B, the reaction conditions for the dehydrogenation reaction are set so as to suppress a decrease in the catalytic activity of the dehydrogenation catalyst and to further increase the yield of hydrogen.

[0033] The reaction temperature in this reactor 13B can be controlled by the amount of heat steadily supplied from the heating furnace 15. In this reactor 13B, hydrogen and toluene are produced from MCH by a dehydrogenation reaction (endothermic reaction), but here, in order to further increase the conversion rate of MCH (i.e., to avoid a decrease in the conversion rate of MCH due to a decrease in the reaction temperature), heat transfer oil at a desired set temperature (about 400°C) is constantly supplied to this reactor 13B from the heating furnace 15, as described above.

[0034] The hydrogen concentration in the product of this reactor 13B is, for example, about 75 vol%, and the MCH conversion rate is 95% or more. However, this is not limiting, and the dehydrogenation reaction in this reactor 13B may be controlled so that the hydrogen concentration in the product is in the range of 60 vol% to 75 vol%, and the MCH conversion rate is 60% or more.

[0035] On the other hand, it is preferable to control the conversion rate of the organic hydride in the preliminary reactor 13A to 10 to 60%, preferably 20 to 50%, and more preferably 25 to 45%. For example, it is preferable to control it to 38 to 42%. If the conversion rate of the organic hydride in the preliminary reactor 13A is estimated to be lower than 50%, it becomes possible to effectively utilize heat of approximately 250°C to 350°C. This increases the variety of external heat sources that can be recovered and effectively utilized by the heat recovery unit 16.

[0036] As described above, the final conversion rate of the organic hydride is determined not by the reaction in the preliminary reactor 13A but by the reaction in the main reactor 13B. In this embodiment, the conversion rate of the organic hydride after passing through the main reactor 13B (the total conversion rate of the preliminary reactor 13A and the main reactor 13B) is controlled to be 60% or more, preferably 80% or more. Even if the reaction temperature in the preliminary reactor 13A becomes lower than the reaction temperature in the main reactor 13B, the final conversion rate of the organic hydride does not decrease.

[0037] When the entire dehydrogenation reaction system 1 is considered, if the conversion of the organic hydride in the preliminary reactor 13A is, for example, about 40% complete, the required amount of heat (heat duty) to be supplied to the main reactor 13B by the heating furnace 15 is reduced by about 40%. The reduction in the required amount of heat to be supplied to the main reactor 13B by the heating furnace 15 varies depending on the conversion rate of the organic hydride in the preliminary reactor 13A, and the greater the conversion rate of the organic hydride in the preliminary reactor 13A, the greater the reduction in the required amount of heat to be supplied to the main reactor 13B by the heating furnace 15.

[0038] Furthermore, since the thermal system of the preliminary reactor 13A and the thermal system of the main reactor 13B are independent of each other, heat management is easy. Therefore, for example, waste of thermal energy, such as providing heat to the preliminary reactor 13A in excess of the conversion rate expected for the amount of catalyst in the preliminary reactor 13A, does not occur. Furthermore, problems such as not achieving the expected conversion rate due to the lack of heat supplied to the main reactor 13B in the required temperature range do not occur. Moreover, the hydrogen generated in the preliminary reactor 13A suppresses a decrease in catalyst activity due to carbon generation near the inlet of the main reactor 13B.

[0039] 2. Second embodiment A dehydrogenation reaction system 1A, which is a variation of the dehydrogenation reaction system 1, will be briefly described using FIG. 2. The basic configuration of the dehydrogenation reaction system 1A is the same as that of the dehydrogenation reaction system 1. In the dehydrogenation reaction system 1A, an adiabatic preliminary reactor 13C and a main reactor 13D are used instead of the multi-tubular preliminary reactor 13A and the main reactor 13B. Also, in the methanation reaction apparatus 2A, an adiabatic methanation reactor 22A is used instead of the multi-tubular methanation reactor 22. Here again, for convenience of explanation, an example in which a single reactor is arranged is shown, but the present invention can also be suitably applied to cases in which the methanation reactors 22A are arranged in multiple stages.

[0040] The preliminary reactor 13C, the main reactor 13D, and the methanation reactor 22A are configured so that heat exchange with the outside does not occur during the reaction. A known adiabatic reactor configuration, in which a catalyst is packed into a catalytic reactor vessel lined with an insulating material, can be used as the adiabatic reactor. The catalytic reactor vessel is configured so that reactants flow from one side of the catalyst layer to the other. By using adiabatic reactors with a relatively simple structure for the preliminary reactor 13C, the main reactor 13D, and the methanation reactor 22A, the manufacturing costs of the dehydrogenation reaction system 1A and the methanation reactor 2A can be reduced. Furthermore, since the methanation reactor 22A, in which an exothermic reaction occurs, tends to have a higher outlet temperature than a multi-tubular reactor, the heat recovery section 16 can recover heat in a higher temperature range.

[0041] When an adiabatic reactor is used, the heat recovery section 16 preferably supplies heat to the inlet side of the preliminary reactor 13C. Similarly, the heating furnace 15 preferably supplies heat to the inlet side of the main reactor 13D. On the other hand, as described above, the heat recovery section 16 preferably recovers heat from the outlet side of the methanation reactor 22A. In FIG. 2, the preliminary reactor 13C, the main reactor 13D, and the methanation reactor 22A are simultaneously used as adiabatic reactors. However, it is also possible to selectively use at least one of these, with the remaining reactors being multi-tubular reactors. For example, the present invention can be suitably applied even when a shell-and-tube methanation reactor 22 and an adiabatic methanation reactor 22A are combined.

[0042] 3. Third embodiment FIG. 3 shows an example in which two preliminary reactors 13A1 and 13A2 and a main reactor 13B are arranged in the dehydrogenation reaction section 13. Here, the heat recovery section 16 supplies heat recovered by the external heat source 2B (e.g., 230°C to 250°C) to the preliminary reactor 13A1, and supplies heat recovered by the external heat source 2C (e.g., 280°C to 300°C) to the preliminary reactor 13A2. When there are multiple external heat sources 2B and 2C with different recoverable heat temperature ranges, it is preferable to supply the heat of the external heat source 2B with a lower temperature range to the upstream preliminary reactor 13A1, and the heat of the external heat source 2C with a higher temperature range to the downstream preliminary reactor 13A2. Heat is stably supplied to the main reactor 13B from a heating furnace 15.

[0043] In this way, by supplying heat to the main reactor 13B, the preliminary reactor 13A1, and the preliminary reactor 13A2 using independent heat systems, it becomes possible to carry out the dehydrogenation reaction using a wider variety of external heat sources while maintaining a high final organic hydride conversion rate. Examples of the external heat source 2B and the external heat source 2C include exhaust gas or exhaust steam from a methanation reactor, a CCU process reactor, other SOFC equipment, combustion heat sources, industrial waste heat sources, etc. When high-temperature exhaust gas or exhaust steam is extracted as a heat source, the heat recovery section 16 may send the high-temperature exhaust gas or exhaust steam directly to the shells of the preliminary reactors 13A1 and 13A2, etc., without using heat transfer oil.

[0044] 4. Other embodiments In the above-described embodiment, an example has been shown in which part of the heat recovered by the heat recovery section 16 is also supplied to the evaporator 11 and the superheater 12. However, heat may also be supplied from the heat recovery section 16 to, for example, a distillation apparatus for separating and removing polymerization products, which are reaction inhibitors, from MCH or toluene. On the other hand, heat may also be supplied to the evaporator 11 and the superheater 12 as appropriate from a heat source other than the heat recovery section 16. [Explanation of symbols]

[0045] 1: Dehydrogenation reaction system 1A: Dehydrogenation reaction system 2: Methanation reactor 2A: Methanation reactor 2B: External heat source 2C: External heat source 4A: Tank 4B: Pump 11: Evaporator 12:Superheater 13: Dehydrogenation reaction section 13A: Pre-reactor 13A1: Pre-reactor 13A2: Pre-reactor 13B: Main reactor 13C: Pre-reactor 13D: Main reactor 14:Separator 15:Heating furnace 16: Heat recovery section 21: Input section 22: Methanation reactor 22A: Methanation reactor 23: 1st separator 24:Second separator

Claims

1. A dehydrogenation reaction system having a preliminary reactor, a main reactor, a heating section, and a heat recovery section, the pre-reactor is configured to produce hydrogen from the vaporized hydrogenated aromatic compound; the reactor is configured to produce hydrogen from the hydrogenated aromatic compounds that have passed through the pre-reactor; the heating section is configured to supply heat to the reactor; The dehydrogenation reaction system, wherein the heat recovery unit is configured to recover heat from an external heat source and supply the recovered heat to the pre-reactor.

2. 2. The dehydrogenation reaction system according to claim 1, The dehydrogenation reaction system, wherein the heat recovery section is configured to recover heat in a temperature range of 250°C to 500°C.

3. 2. The dehydrogenation reaction system according to claim 1, a dehydrogenation reaction system, wherein the pre-reactor is a multi-tube reactor having a cylindrical shell and a plurality of tubes extending within the shell;

4. 2. The dehydrogenation reaction system according to claim 1, The dehydrogenation reaction system, wherein the heat recovery section is configured to supply heat from the external heat source to the pre-reactor via hot oil.

5. 2. The dehydrogenation reaction system according to claim 1, The dehydrogenation reaction system is configured so that the heat recovery unit also supplies heat to other heat demand units other than the main reactor.

6. 2. The dehydrogenation reaction system according to claim 1, a dehydrogenation reaction system, wherein the external heat source is heat generated by an exothermic reaction in a methanation reaction section;

7. 7. The dehydrogenation reaction system according to claim 6, The methanation reaction section comprises a multi-tubular reactor having a cylindrical shell and a plurality of tubes extending within the shell.

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