JP2016050143A - Dehydrogenation system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a dehydrogenation system capable of improving the conversion ratio while suppressing caulking.SOLUTION: There is provide a dehydrogenation system 3 which comprises a dehydrogenation reactor 30 and a heating mechanism 22 for supplying heat to the dehydrogenation reactor 30. The dehydrogenation reactor 30 has reaction vessels 31A and 31B in which a raw material containing MCH is circulated and dehydrogenation catalysts 32A and 32B which are located in the reaction vessels and convert MCH into hydrogen and a dehydrogenated product by dehydrogenation reaction. A first part 30A in the dehydrogenation reactor 30 is heated by supplying a heat medium heated to a predetermined heating temperature by supplying a first heat source 41A to a first heat exchanger 42A and a second part 30B on the downstream side in the circulation direction of a raw material from the first part 30A is heated by supplying a heat medium heated to a heating temperature higher than that of the first heat source 41A to a second heat exchanger 42B by a second heat source 41B.SELECTED DRAWING: Figure 2

Description

  The present invention relates to a dehydrogenation system that performs a dehydrogenation reaction.

  As a conventional dehydrogenation system, a system is known that generates hydrogen by dehydrogenating a methylcyclohexane supplied by a supply device with a dehydrogenation catalyst in a dehydrogenation reactor (for example, Patent Document 1). The dehydrogenation system described in Patent Document 1 includes a heating mechanism that supplies heat to the dehydrogenation reactor.

JP 2011-251858 A

  In recent years, in the dehydrogenation system, further improvement in the conversion rate from raw material to hydrogen is expected. Since the dehydrogenation reaction is an endothermic reaction, in order to improve the conversion rate in the dehydrogenation system described in Patent Document 1, the heat supply to the dehydrogenation reactor by the heating mechanism is increased to increase the conversion rate. It is conceivable to increase the heating temperature of the elementary reactor. However, when the heating temperature is increased, carbon deposition (coking) tends to occur on the surface of the dehydrogenation catalyst.

  An object of this invention is to provide the dehydrogenation system which can improve a conversion rate, suppressing coking.

  A dehydrogenation system according to the present invention includes a reaction vessel in which a raw material containing an organic hydride circulates, and a dehydration that is located in the reaction vessel and converts the organic hydride into hydrogen and a dehydrogenated product by a dehydrogenation reaction. A dehydrogenation reactor having a hydrogenation catalyst, and a heating unit that supplies heat to the dehydrogenation reactor, the heating unit comprising: a first heating unit that heats a first part of the dehydrogenation reactor; A second heating part for heating the second part downstream in the flow direction of the raw material from the first part in the dehydrogenation reactor, and the heating temperature of the second heating part is that of the first heating part It is higher than the heating temperature.

  In this dehydrogenation system, the heating temperature of the second heating part is higher than the heating temperature of the first heating part, so that the activity of the dehydrogenation reaction in the second part is higher than the activity of the dehydrogenation reaction in the first part. Can be increased. In addition, since the fluid flowing through the second part contains hydrogen obtained by the dehydrogenation reaction in the first part, even if the heating temperature of the second part is raised above the heating temperature of the first part, The occurrence of coking can be suppressed. Therefore, according to the present invention, it is possible to improve the conversion rate while suppressing coking.

  In the dehydrogenation system according to the present invention, the reaction vessel has a first vessel and a second vessel, the first vessel is located in the first part of the dehydrogenation reactor, and the second vessel is dehydrogenated. It may be located in the second part of the conversion reactor. According to such a configuration, for example, when the dehydrogenation catalyst located in the second portion is deteriorated, it is possible to selectively replace only the second container. For example, the heating temperature of the second portion is further increased. The dehydrogenation catalyst located in the first container can be effectively utilized while increasing the conversion rate and increasing the conversion rate.

  In the dehydrogenation system according to the present invention, the average flow rate of the fluid containing the raw material flowing through the inside of the reaction vessel located in the second part is the average flow velocity of the fluid containing the raw material flowing through the inside of the reaction vessel located in the first part. You may be comprised so that it may become larger than an average flow velocity. According to such a configuration, in the reaction vessel located in the second portion, since the thickness of the boundary film, which is generally a region where coking is likely to occur, can be further reduced, while further suppressing coking, The conversion rate can be improved.

  In the dehydrogenation system according to the present invention, the internal pressure of the reaction vessel located in the second part may be configured to be lower than the internal pressure of the reaction vessel located in the first part. According to such a configuration, it is possible to further increase the conversion rate while suppressing coking.

  In the dehydrogenation system according to the present invention, the internal pressure of the reaction vessel located in the second part may be configured to be higher than the internal pressure of the reaction vessel located in the first part. According to such a configuration, coking in the second portion can be further suppressed.

  ADVANTAGE OF THE INVENTION According to this invention, it becomes possible to provide the dehydrogenation system which can improve a conversion rate, suppressing coking.

It is a block diagram which shows the structure of a hydrogen supply system provided with the dehydrogenation system which concerns on 1st Embodiment. It is a block diagram which shows the structure of the dehydrogenation system which concerns on 1st Embodiment. It is a block diagram which shows the structure of the dehydrogenation system which concerns on 2nd Embodiment. (A) is a block diagram which shows a part of dehydrogenation system which concerns on 3rd Embodiment, (b) is a block diagram which shows a part of dehydrogenation system which concerns on 4th Embodiment. It is a block diagram which shows a part of dehydrogenation system which concerns on 5th Embodiment.

  DESCRIPTION OF EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. In the following description, the same or corresponding parts are denoted by the same reference numerals, and redundant description may be omitted.

  FIG. 1 is a block diagram illustrating a configuration of a hydrogen supply system including a dehydrogenation system according to the present embodiment. A hydrogen supply system 100 shown in FIG. 1 uses organic hydride as a raw material for generating hydrogen to be supplied. The organic hydride can be transported to the hydrogen supply system 100 as a liquid fuel by a tank lorry as in the case of gasoline.

  An organic hydride is a hydride of an organic compound having an unsaturated bond, and is converted into a dehydrogenation reaction product containing hydrogen and a dehydrogenated product (an organic compound having an unsaturated bond) using a dehydrogenation catalyst. be able to. In the present embodiment, methylcyclohexane (hereinafter referred to as “MCH”) is used as the organic hydride, but is not limited thereto. Examples of hydrogen used for producing organic hydride include hydrogen produced in large quantities at refineries, hydrogen generated by electrolysis of water using natural energy, and the like. Is not limited.

  An organic compound having an unsaturated bond is an organic compound having one or more double bonds or triple bonds in the molecule. As the double bond, carbon-carbon double bond (C = C), carbon-nitrogen double bond (C = N), carbon-oxygen double bond (C = O), nitrogen-oxygen double bond (N = O). Examples of the triple bond include a carbon-carbon triple bond and a carbon-nitrogen triple bond. The organic compound having an unsaturated bond is preferably a liquid organic compound under normal temperature and pressure from the viewpoint of storage properties and transportability.

  Examples of the organic compound having an unsaturated bond include olefins, dienes, acetylenes, benzene, carbon chain-substituted aromatics, hetero-substituted aromatics, polycyclic aromatics, Schiff bases, and heteroaromatics. , Hetero 5-membered ring compounds, quinones, ketones and the like. Examples of olefins include ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, and the like. Examples of dienes include allene, butadiene, pentadiene, hexadiene, hebutadiene, octadiene, piperylene, isoprene and the like. Examples of acetylenes include acetylene, propyne, and vinyl acetylene. Examples of the carbon chain substituted aromatics include alkyl substituted aromatics. Examples of the alkyl-substituted aromatics include toluene, xylene, trimethylbenzene, ethylbenzene, cumene, benzoic acid and the like. Examples of hetero-substituted aromatics include anisole, dimethoxybenzene, phenol, aniline, N, N-dimethylaniline and the like. Examples of polycyclic aromatics include naphthalene, methylnaphthalene, anthracene, tetracene, phenanthrene, tetralin, and azulene. Examples of Schiff bases include 2-aza-hept-1-en-1-yl-cyclohexane. Heteroaromatics include pyridine, pyrimidine, quinoline, isoquinoline and the like. Examples of hetero 5-membered ring compounds include furan, thiophene, pyrrole, and imidazole. Examples of quinones include benzoquinone and naphthoquinone. Examples of ketones include acetone and methyl ethyl ketone. Needless to say, carbon dioxide and carbon monoxide have an unsaturated bond, but are generally not regarded as organic compounds, and thus are excluded from the organic compounds having an unsaturated bond in the present embodiment.

  Among the above unsaturated compounds, benzene, toluene, xylene, ethylbenzene, naphthalene, methylnaphthalene, tetralin and the like (hereinafter referred to as “benzene”) are water-insoluble before and after hydrogenation, and are phase separated from water. Since it is possible, it is preferable to water-soluble organic compounds such as acetone from the viewpoint of easy recovery as a product. The water-insoluble organic compound may be one kind of compound such as benzene or a mixture of two or more kinds.

  The hydrogen supply system 100 has a function of supplying hydrogen to, for example, a fuel cell vehicle (hereinafter referred to as “FCV”) or a hydrogen engine vehicle.

  In the present embodiment, the hydrogen supply system 100 will be described using a hydrogen station that supplies high-purity hydrogen to the FCV as an example. As shown in FIG. 1, the hydrogen supply system 100 according to the present embodiment includes a raw material tank 1, a vaporizer 2, a dehydrogenation system 3, a separator 4, a recovery tank 5, a hydrogen purifier 6, a compressor 7, an accumulator. The container 8, the dispenser 9, and the cooling-heat source 13 are provided, and each component is connected through the lines L1-L9.

  The line L1 connects the raw material tank 1 and the vaporizer 2. Line L2 connects the vaporizer 2 and the dehydrogenation system 3. A line L3 connects the dehydrogenation system 3 and the separator 4. Line L4 connects separator 4 and hydrogen purifier 6. The line L5 connects the separator 4 and the recovery tank 5. The line L6 connects the hydrogen purifier 6 and the compressor 7. The line L7 connects the hydrogen purifier 6 and the vaporizer 2. The line L8 connects the compressor 7 and the pressure accumulator 8. Line L9 connects pressure accumulator 8 and dispenser 9.

  The raw material tank 1 has a function of storing MCH as a raw material in the present embodiment. The MCH stored in the raw material tank 1 is transported from the outside by a tank lorry or the like, and supplied to the vaporizer 2 via the line L1 by a compressor (not shown), for example.

  The vaporizer 2 has a function of vaporizing the MCH supplied from the raw material tank 1. The MCH vaporized by the vaporizer 2 is supplied to the dehydrogenation system 3 via the line L2.

  The dehydrogenation system 3 has a function of generating a dehydrogenation reaction product (hydrogen-containing gas) by causing a dehydrogenation reaction of MCH. The dehydrogenation reaction product according to the present embodiment is mainly composed of hydrogen and toluene (dehydrogenation product) produced by dehydrogenation reaction of MCH, and in some cases, the dehydrogenation reaction is not performed. MCH (unreacted material) and impurities. The dehydrogenation reaction product generated by the dehydrogenation system 3 is supplied to the separator 4 via the line L3.

  The separator 4 has a function of separating toluene, which is a dehydrogenated product, from the dehydrogenated reactant, and examples thereof include a gas-liquid separator. When a gas-liquid separator is employed as the separator 4, for example, by cooling the dehydrogenation reactant supplied from the dehydrogenation system 3 via the line L 3, the dehydrogenated toluene or unreacted material is used. Since certain MCH can be preferentially liquefied, it can be gas-liquid separated from hydrogen, which is relatively difficult to liquefy. The cooling temperature in this gas-liquid separator is preferably lower (for example, 50 ° C. or lower) from the viewpoint of separation efficiency. The pressure in the gas-liquid separator is preferably higher (for example, 0.2 MPa to 1.0 MPa) from the viewpoint of promoting liquefaction of toluene, which is a dehydrogenated product. Toluene, which is a dehydrogenated product separated by the separator 4, and MCH, which is an unreacted product, are supplied to the recovery tank 5 through a line L5. The hydrogen-containing gas obtained by separating toluene and MCH with the separator 4 is supplied to the hydrogen purifier 6 via the line L4.

  The recovery tank 5 has a function of storing toluene and MCH separated by the separator 4. For example, toluene collected in the collection tank 5 is transported to a refinery or the like by a tank lorry, hydrogenated again, and converted into MCH.

  The hydrogen purifier 6 further removes dehydrogenated toluene, unreacted MCH, and the like from the hydrogen-containing gas supplied from the separator 4, and increases the hydrogen purity to the extent required by FCV, for example. It has a function. High purity hydrogen (purified gas) obtained by the hydrogen purifier 6 is supplied to the compressor 7 directly or indirectly via the line L6. Here, indirect means, for example, temporarily storing high-purity hydrogen in a tank or the like. On the other hand, off-gas containing toluene, which is a dehydrogenated product removed by the hydrogen purifier 6, and MCH, which is an unreacted product, is supplied to the line L7 together with hydrogen that cannot be recovered as a purified gas in the hydrogen purifier 6. . The off gas supplied to the line L7 is supplied to the vaporizer 2 through a compressor (not shown), for example, and dehydrated through the line L2 together with the raw material (MCH) supplied from the raw material tank 1 and vaporized in the vaporizer 2. The raw material is supplied to the raw material system 3. Even when off-gas is mixed with the raw material and supplied to the dehydrogenation system 3, there may be a case where the raw material is simply described as “supply the raw material to the dehydrogenation system 3”.

  Examples of the hydrogen purifier 6 include a membrane separation apparatus including a hydrogen separation membrane, an adsorption removal apparatus using a PSA (Pressure swing adsorption) method or a TSA (Temperature swing adsorption) method.

  The compressor 7 has a function of making the high-purity hydrogen obtained by the hydrogen purifier 6 into a higher pressure (for example, 20 MPa to 90 MPa). The high-purity hydrogen brought to a high pressure state by the compressor 7 is supplied to the pressure accumulator 8 via the line L8. In the present embodiment, the high-purity hydrogen that has been brought into a high pressure state by the compressor 7 is supplied to the accumulator 8. However, the present invention is not limited to this. For example, the high-purity hydrogen in the high-pressure state is dispensed directly. 9 may be supplied.

  The pressure accumulator 8 has a function of storing high purity hydrogen in a high pressure state. High-purity hydrogen stored in the accumulator 8 in a high pressure state is supplied to the FCV by the dispenser 9 via the line L9. In the present embodiment, for example, from the viewpoint of making it possible to increase the hydrogen supply speed to the FCV, the high-purity hydrogen passing through the line L9 is cooled by the cold heat source 13. However, the present invention is not limited to this, and the cold heat source 13 may be adopted.

  Next, the configuration of the dehydrogenation system 3 will be specifically described.

  FIG. 2 is a block diagram showing a configuration of the dehydrogenation system 3 according to the first embodiment. As shown in FIG. 2, the dehydrogenation system 3 includes a dehydrogenation reactor 30, a raw material supply mechanism 21, a heating mechanism 22, a pressure reducing valve 23, and a control unit 24.

  The dehydrogenation reactor 30 is divided into a first portion 30A located upstream and a second portion 30B located downstream from the first portion 30A in the flow direction of the raw material supplied from the raw material supply mechanism 21. It is divided and configured. The position where the first part 30A and the second part 30B are separated in the dehydrogenation reactor 30 is set, for example, based on the reaction conditions such as pressure and temperature in the second part 30B, but coking in the second part 30B. From the viewpoint of more appropriately suppressing the MCH conversion rate at the downstream end of the first portion 30A is 50% or more, particularly the temperature at the second portion 30B, for example, the temperature at which pyrolysis of petroleum-derived hydrocarbons accelerates (for example, 350 ° C. ) Is preferably set at a position where the conversion rate is 70% or more. The dehydrogenation reactor 30 in the present embodiment is configured to be divided into two parts, the first part 30A and the second part 30B, but is not limited to this, and is divided into three or more parts. It is good also as a structure.

  The dehydrogenation reactor 30 includes reaction vessels 31A and 31B, dehydrogenation catalysts 32A and 32B, distribution units 34A and 34B, aggregation units 37A and 37B, and a communication pipe 38. In the dehydrogenation reactor 30, the reaction vessel 31A, the dehydrogenation catalyst 32A, the distribution unit 34A, and the aggregation unit 37A are located in the first portion 30A, and the reaction vessel 31B, the dehydrogenation catalyst 32B, and the distribution unit 34B. And the consolidating part 37B are located in the second portion 30B.

  The reaction vessel 31 </ b> A is configured such that the raw material circulates inside. Although reaction container 31A in this embodiment is comprised including the some reaction tube 35A arrange | positioned in parallel, it is not restricted to such a structure. The shape of the reaction tube 35A in the present embodiment is a cylindrical shape, but is not limited thereto, and may be, for example, a double tubular shape, a box shape, or a honeycomb shape.

  The dehydrogenation catalyst 32A has a function of converting MCH into hydrogen and a dehydrogenated product by a dehydrogenation reaction. The dehydrogenation catalyst 32A in the present embodiment is located inside each reaction tube 35A constituting the reaction vessel 31A. Examples of the dehydrogenation catalyst 32A include a catalyst in which a catalyst metal such as platinum, ruthenium, palladium, rhodium, tin, rhenium or germanium is supported on a porous carrier such as alumina. The shape of the dehydrogenation catalyst 32A is not particularly limited, and examples thereof include a columnar shape and a honeycomb shape.

  The distribution unit 34A has a function of distributing the raw material supplied from the vaporizer 2 (see FIG. 1) via the line L2 to each reaction tube 35A while adjusting the supply amount by the raw material supply mechanism 21. The first portion 30A is located at the upstream end of each reaction tube 35A. The distributor 34A has an inlet 36 through which the raw material supplied from the raw material supply mechanism 21 flows through the line L2.

  The concentrating part 37A is generated by dehydrogenating a part of the raw material with the dehydrogenation catalyst 32A located in the reaction vessel 31A, and the raw material and dehydration discharged from each reaction tube 35A constituting the reaction vessel 31A. It has a function of consolidating the first fluid containing the raw reactant (hydrogen-containing gas), and is located at the downstream end of each reaction tube 35A in the first portion 30A. The aggregation portion 37A has a discharge port 33A for discharging the first fluid described above to the communication pipe 38.

  The reaction vessel 31B is configured such that the above-described first fluid supplied from the first portion 30A through the communication pipe 38 flows inside. Although reaction container 31B in this embodiment is comprised including the some reaction tube 35B arrange | positioned in parallel, it is not restricted to such a structure. The shape of the reaction tube 35B in the present embodiment is a cylindrical shape, but may be, for example, a double tubular shape, a box shape, or a honeycomb shape. In the present embodiment, the reaction tube 35A constituting the reaction vessel 31A and the reaction tube 35B constituting the reaction vessel 31B are configured to have the same number of tubes and the same tube diameter.

  The dehydrogenation catalyst 32B has a function of converting MCH into hydrogen and a dehydrogenated product by a dehydrogenation reaction. The dehydrogenation catalyst 32B in the present embodiment is located inside each reaction tube 35B constituting the reaction vessel 31B. Examples of the dehydrogenation catalyst 32B include a catalyst in which a catalyst metal such as platinum, ruthenium, palladium, rhodium, tin, rhenium, or germanium is supported on a porous carrier such as alumina. The shape of the dehydrogenation catalyst 32B is not particularly limited, and examples thereof include a columnar shape and a honeycomb shape. In the present embodiment, the catalyst amount of the dehydrogenation catalyst 32B located in the reaction vessel 31B is the same as that of the dehydrogenation catalyst 32A located in the reaction vessel 31A from the viewpoint of suppression of coking and reduction in energy efficiency. The structure is less than the catalyst amount.

  The distribution unit 34B has a function of distributing the first fluid supplied from the first part 30A via the communication pipe 38 to the reaction tubes 35B. The distribution part 34B has a function of distributing each reaction tube 35B in the second part 30B. Located at the upstream end. The distributor 34B is connected to the communication pipe 38 and has a supply port 33B to which the first fluid is supplied.

  The aggregating portion 37B is generated by dehydrogenating the raw material with the dehydrogenation catalyst 32B located in the reaction vessel 31B, and dehydrogenation reactants discharged from the respective reaction tubes 35B constituting the reaction vessel 31B ( The second fluid containing the hydrogen-containing gas) has a function of aggregating, and is located at the downstream end of each reaction tube 35B in the second portion 30B. The aggregation part 37B has a discharge port 39 for discharging the second fluid described above to the line L3.

  The raw material supply mechanism 21 has a function of adjusting the raw material supply to the inlet 36 in the dehydrogenation reactor 30 based on a control signal from the control unit 24. The raw material supply mechanism 21 in this embodiment includes a pump (not shown) for supplying the raw material from the raw material tank 1 via the line L1, and a flow rate adjusting valve (not shown) for adjusting the supply amount of the raw material. However, the present invention is not limited to such a configuration.

  The heating mechanism 22 has a function of supplying heat to the dehydrogenation reactor 30. The heating mechanism 22 in the present embodiment includes a first heat source 41A, a second heat source 41B, a first heat exchanger (first heating unit) 42A, and a second heat exchanger (second heating unit) 42B. It is configured to include.

  The first heat source 41A has a function of heating the heat medium supplied to the first heat exchanger 42A. The heating temperature of the heat medium in the first heat source 41A is set so that the final conversion rate of MCH in the first portion 30A of the dehydrogenation reactor 30 becomes a predetermined reference value (for example, 50% to 95%), For example, the temperature is set to 340 ° C. to 350 ° C. at the inlet 43A (described later) of the first heat exchanger 42A. Further, the first heat source 41A in the present embodiment has a function of supplying the heat medium heated by the first heat source 41A to the first heat exchanger 42A, but is not limited to such a configuration. A pump that supplies a heat medium to the first heat exchanger 42A may be arranged separately from the first heat source 41A. In the present embodiment, from the viewpoint of ease of control of the final conversion rate of MCH in the first portion 30A of the dehydrogenation reactor 30, the heat temperature at the inlet 43A is used as the heating temperature of the heat medium in the first heat source 41A. Although the temperature of the medium is adopted, the present invention is not limited to this, and the temperature of the heat medium at the outlet 44A may be adopted, or a temperature based on the temperature of the heat medium at both the inlet 43A and the outlet 44A may be adopted. Alternatively, a temperature based on the temperature of the heat medium at one or a plurality of arbitrary locations may be adopted.

  The first heat exchanger 42A includes a heat medium supplied from the first heat source 41A and each reaction tube 35A (and thus a dehydrogenation catalyst located in each reaction tube 35A) constituting the reaction vessel 31A of the first portion 30A. 32A and the like). The first heat exchanger 42A has an inlet 43A and an outlet 44A, and is located so as to surround a region where the dehydrogenation catalyst 32A is located in the reaction vessel 31A. The first heat exchanger 42A may have a configuration such as a baffle plate or a fin in order to appropriately perform heat exchange between the heat medium and each reaction tube 35A.

  The inflow port 43A is for allowing the heat medium supplied from the first heat source 41A to flow into the first heat exchanger 42A, and is located near the downstream end of the reaction vessel 31A. The discharge port 44A is for discharging the heat medium in the first heat exchanger 42A to the outside of the first heat exchanger 42A, and is located near the upstream end of the reaction vessel 31A. According to such a configuration, the temperature on the downstream side can be made higher than that on the upstream side of the reaction vessel 31A, which is suitable for increasing the conversion rate of MCH. Note that the configuration of the first heat exchanger 42A is not limited to that described above. For example, the inlet 43A is disposed near the upstream end of the reaction vessel 31A, and the outlet 44A is the downstream end of the reaction vessel 31A. It is good also as a structure arrange | positioned in the vicinity of a part.

  The second heat source 41B has a function of heating the heat medium supplied to the second heat exchanger 42B. The heating temperature of the heat medium in the second heat source 41B is set so that the final conversion rate of MCH in the second portion 30B of the dehydrogenation reactor 30 becomes a predetermined reference value (for example, 90% to 99%). The temperature is set to be higher than the heating temperature of the heat medium in the heat source 41A, and is set to, for example, 370 ° C. to 380 ° C. at the inlet 43B (described later) of the second heat exchanger 42B. Further, the second heat source 41B in the present embodiment has a function of supplying the heat medium heated by the second heat source 41B to the second heat exchanger 42B, but is not limited to such a configuration. The pump that supplies the heat medium to the two heat exchangers 42B may be arranged separately from the second heat source 41B. In the present embodiment, from the viewpoint of easy control of the final conversion rate of MCH in the second portion 30B of the dehydrogenation reactor 30, the heating temperature of the heat medium at the second heat source 41B is used as the heat temperature at the inlet 43B. Although the temperature of the medium is adopted, the present invention is not limited to this, and the temperature of the heat medium at the outlet 44B may be adopted, or a temperature based on the temperature of the heat medium at both the inlet 43B and the outlet 44B may be adopted. Alternatively, a temperature based on the temperature of the heat medium at one or a plurality of arbitrary locations may be adopted.

  The second heat exchanger 42B includes a heat medium supplied from the second heat source 41B, and each reaction tube 35B (and thus a dehydrogenation catalyst located in each reaction tube 35B) constituting the reaction vessel 31B of the second portion 30B. 32B and the like). The second heat exchanger 42B has an inlet 43B and an outlet 44B, and is located so as to surround a region where the dehydrogenation catalyst 32B is located in the reaction vessel 31B. The second heat exchanger 42B may have a configuration such as a baffle plate or a fin in order to appropriately perform heat exchange between the heat medium and each reaction tube 35B.

  The inflow port 43B is for allowing the heat medium supplied from the second heat source 41B to flow into the second heat exchanger 42B, and is located near the downstream end of the reaction vessel 31B. The discharge port 44B is for discharging the heat medium in the second heat exchanger 42B to the outside of the second heat exchanger 42B, and is located in the vicinity of the upstream end of the reaction vessel 31B. According to such a configuration, since the temperature on the downstream side can be made higher than that on the upstream side of the reaction vessel 31B, it is suitable for increasing the conversion rate of MCH. Note that the configuration of the second heat exchanger 42B is not limited to that described above. For example, the inlet 43B is disposed near the upstream end of the reaction vessel 31B, and the outlet 44B is the downstream end of the reaction vessel 31B. It is good also as a structure arrange | positioned in the vicinity of a part.

  The heating mechanism 22 is not limited to the above-described configuration as long as the heating temperature for heating the second portion 30B is higher than the heating temperature for heating the first portion 30A. It is good also as a structure by the electric heater arrange | positioned so that the predetermined location of the part 30A and the 2nd part 30B may be enclosed.

  The pressure reducing valve 23 functions to adjust the internal pressure of the reaction vessel 31B located in the second portion 30B in the dehydrogenation reactor 30 to be lower than the internal pressure of the reaction vessel 31A located in the first portion 30A. It is located in the communication pipe 38 that connects the concentrating part 37A and the distributing part 34B. The pressure reducing valve 23 in the present embodiment gives a pressure difference (pressure loss) between the upstream side and the downstream side by restricting the flow path of the communication pipe 38, and the reaction vessel 31B located in the second portion 30B. Reduce the internal pressure. Further, the pressure reducing valve 23 in the present embodiment has a function of changing the valve opening according to the pressure on the downstream side of the pressure reducing valve 23, and even when the pressure on the downstream side fluctuates, The internal pressure of the reaction vessel 31B located in the second portion 30B is controlled to be lower than the internal pressure of the first portion 30A.

  In the dehydrogenation system 3, when the MCH is dehydrogenated to generate a dehydrogenation reaction product, the pressure reducing valve 23 is driven and flows from the first part 30 </ b> A to the second part 30 </ b> B via the communication pipe 38. The fluid to be reduced is depressurized by the pressure reducing valve 23. Thereby, the pressure of the fluid flowing through each reaction tube 35B constituting the reaction vessel 31B becomes lower than the pressure of the fluid flowing through each reaction tube 35A constituting the reaction vessel 31A. As the pressure reducing valve 23, for example, either a direct acting type or a pilot type can be adopted.

  In addition, as long as it can reduce the internal pressure of reaction container 31B located in the 2nd part 30B, it may replace with the pressure reduction valve 23, and may employ | adopt another mechanism and structure. For example, a pressure sensor that detects the internal pressure of the reaction vessel 31B located in the second portion 30B and a control valve that restricts the flow path of the fluid from the first portion 30A to the second portion 30B are provided. Based on the value, the valve opening degree of the control valve may be controlled so that the internal pressure of the reaction vessel 31B located in the second portion 30B becomes low. In addition to the pressure reducing valve 23, a suction pump, a compressor, and the like are provided downstream of the discharge port 39 so that the internal pressure of the reaction vessel 31B located in the second portion 30B is the reaction vessel 31A located in the first portion 30A. The internal pressure may be controlled independently of the internal pressure.

  The control unit 24 has a function of transmitting a control signal for controlling each component constituting the dehydrogenation system 3, and includes, for example, a central processing unit (CPU), a storage medium, and a display device. Yes. The control unit 24 in the present embodiment performs control related to the dehydrogenation reaction in the dehydrogenation reactor 30 during the system operation of the dehydrogenation system 3, for example. Specifically, the control unit 24 supplies the raw material to the dehydrogenation reactor 30 by controlling the raw material supply mechanism 21, and controls each heat medium by controlling the first heat source 41A and the second heat source 41B. Heat is supplied to the dehydrogenation reactor 30 through the heat exchanger. The control unit 24 may have a function for controlling the entire hydrogen supply system 100 shown in FIG.

  Next, the operation and effect of the dehydrogenation system 3 according to the present embodiment will be described.

  In the dehydrogenation system 3 configured as described above, the first portion 30A of the dehydrogenation reactor 30 (here, each reaction tube 35A constituting the reaction vessel 31A) is heated to a predetermined temperature by the first heat source 41A. The second part 30B of the dehydrogenation reactor 30 (here, each reaction tube 35B constituting the reaction vessel 31B) is heated by the heat medium heated to the temperature, and the first heat source 41A is heated by the second heat source 41B. It is heated by a heating medium heated to a heating temperature higher than the temperature. Thereby, the activity of the dehydrogenation reaction in the second portion 30B can be increased more than the activity of the dehydrogenation reaction in the first portion 30A. In addition, since the raw material is supplied to the second portion 30B together with the hydrogen obtained by the dehydrogenation reaction in the first portion 30A, coking occurs even when the heating temperature of the second portion 30B is increased. It is hard to do. Therefore, according to the dehydrogenation system 3, it is possible to improve the conversion rate while suppressing coking.

Further, in the dehydrogenation system 3, the activity of the dehydrogenation reaction in the second portion 30B can be increased from the activity of the dehydrogenation reaction in the first portion 30A. Compared to the case where both the portion 30A and the second portion 30B are heated at the heating temperature of the first heat source 41A, the catalyst amounts of the dehydrogenation catalysts 32A and 32B necessary to obtain a predetermined target conversion rate can be reduced. For example, the final conversion rate of MCH in the second portion 30B of the dehydrogenation reactor 30 is 95%, the amount of hydrogen produced is 300 m ³ / h, the heating temperature in the first heat source 41A is 350 ° C., and the second heat source 41B When the heating temperature of 380 ° C. was set to 380 ° C., it was confirmed that the required catalyst amount of the dehydrogenation catalysts 32A and 32B could be reduced by about 40%. Therefore, in the dehydrogenation system 3, the size of the system can be reduced.

  The dehydrogenation reactor 30 of the dehydrogenation system 3 is divided into a reaction vessel 31A located in the first portion 30A and a reaction vessel 31B located in the second portion 30B. Therefore, in the dehydrogenation system 3, for example, when the dehydrogenation catalyst 32B of the reaction vessel 31B located in the second portion 30B deteriorates, only the reaction vessel 31B located in the second portion 30B can be selectively replaced. Therefore, for example, the dehydrogenation catalyst 32A located in the reaction vessel 31A can be effectively used while further increasing the heating temperature of the second portion 30B to further improve the conversion rate.

  When the internal pressure (hydrogen partial pressure) of the reaction vessel in the dehydrogenation reactor is lowered, there is a tendency that coking is likely to occur while the conversion rate is improved. In the second portion 30B in the dehydrogenation system 3, since the raw material is supplied together with the hydrogen obtained by the dehydrogenation reaction in the first portion 30A as described above, the reaction vessel 31B in the second portion 30B is supplied. Even if the internal pressure is reduced, it is difficult for coking to occur. Therefore, in the dehydrogenation system 3, by reducing the internal pressure of the reaction vessel 31B in the second portion 30B by the pressure reducing valve 23, the heating temperature of the second portion 30B is set relatively high while suppressing coking. The conversion rate can be further increased together with the improvement in conversion rate. In addition, although the dehydrogenation system 3 in this embodiment is set as the structure provided with the pressure-reducing valve 23, it does not necessarily need to be equipped with the pressure-reducing valve 23. FIG.

  In the dehydrogenation system 3, the first portion 30A has an aggregation part 37A. Thereby, since the 1st fluid discharged | emitted from each reaction tube 35A which comprises reaction container 31A can be mixed in the aggregation part 37A before making it flow in into the 2nd part 30B, it finally becomes 2nd part 30B. Variations in temperature and composition of the second fluid discharged from each reaction tube 35B constituting the reaction vessel 31B positioned can be reduced. As a result, the dehydrogenation system 3 can improve the conversion rate.

[Second Embodiment]
Next, the dehydrogenation system 203 according to the second embodiment will be described. Below, a different point from the dehydrogenation system 3 which concerns on 1st Embodiment is demonstrated, and the overlapping description may be abbreviate | omitted.

  FIG. 3 is a block diagram showing a configuration of the dehydrogenation system 203 according to the second embodiment. As shown in FIG. 3, the dehydrogenation system 203 uses a dehydrogenation reactor 230 and a heating mechanism 222 in place of the dehydrogenation reactor 30 and the heating mechanism 22 (see FIG. 2). Different from system 3. Other configurations of the dehydrogenation system 203 are the same as those described above with respect to the dehydrogenation system 3.

  In the dehydrogenation reactor 230, in the flow direction of the raw material supplied from the raw material supply mechanism 21, the first portion 30A located on the upstream side and the second portion 30B located on the downstream side from the first portion 30A are integrated. It is structured. The position where the first part 30A and the second part 30B are separated in the dehydrogenation reactor 230 is set based on the reaction conditions such as pressure and temperature in the second part 30B, for example, but the coking in the second part 30B is performed. MCH conversion at the downstream end of the first portion 30A is 50% or more from the viewpoint of suppressing the temperature, in particular, the temperature in the second portion 30B exceeds the temperature at which the pyrolysis of petroleum-derived hydrocarbons accelerates (eg, 350 ° C.). When the temperature is set, it is preferable to set the conversion rate at a position of 70% or more.

  The dehydrogenation reactor 230 includes a reaction vessel 31, a dehydrogenation catalyst 32, a distribution unit 34, and an aggregation unit 37. In the dehydrogenation reactor 230, the upstream side of the reaction vessel 31 and the dehydrogenation catalyst 32 and the distribution unit 34 are located in the first portion 30 </ b> A, and the downstream side of the reaction vessel 31 and the dehydrogenation catalyst 32. The aggregation unit 37 is located in the second portion 30B.

  The reaction vessel 31 is configured such that the raw material circulates inside. Although the reaction container 31 in this embodiment is comprised including the some reaction tube 35 arrange | positioned in parallel, it is not restricted to such a structure. Examples of the reaction tube 35 in the present embodiment include the same ones as the reaction tubes 35A and 35B.

  The dehydrogenation catalyst 32 has a function of converting MCH into hydrogen and a dehydrogenated product by a dehydrogenation reaction. In the present embodiment, the dehydrogenation catalyst 32 is located inside each reaction tube 35 constituting the reaction vessel 31. Examples of the dehydrogenation catalyst 32 include those similar to the dehydrogenation catalysts 32A and 32B.

  The distribution unit 34 has a function of distributing the raw material supplied from the vaporizer 2 (see FIG. 1) via the line L2 to each reaction tube 35 while adjusting the supply amount by the raw material supply mechanism 21. , Located at the upstream end of each reaction tube 35A. The distributor 34 has an inlet 36 through which the raw material supplied from the raw material supply mechanism 21 flows through the line L2.

  The aggregating unit 37 is generated by dehydrogenating a raw material with a dehydrogenation catalyst 32 located in the reaction vessel 31, and dehydrogenated reactants discharged from each reaction tube 35 constituting the reaction vessel 31 ( It has a function of collecting a fluid containing a hydrogen-containing gas) and is located at the downstream end of each reaction tube 35. The aggregation part 37 has a discharge port 39 for discharging the fluid described above to the line L3.

  The heating mechanism 222 has a function of supplying heat to the dehydrogenation reactor 30. The heating mechanism 222 in this embodiment includes a first heat source 41A, a second heat source 41B, a first heat exchanger (first heating unit) 42A, and a second heat exchanger (second heating unit) 42B. It is configured to include. The heating mechanism 222 in the present embodiment is different from the heating mechanism 22 (see FIG. 2) in that the first heat exchanger 42A and the second heat exchanger 42B are disposed adjacent to each other.

  The first heat exchanger 42A includes a heat medium supplied from the first heat source 41A, and each reaction tube 35 (and thus a dehydrogenation catalyst located in each reaction tube 35) constituting the reaction vessel 31 in the first portion 30A. 32) and the like. The first heat exchanger 42A has an inlet 43A and an outlet 44A, and is positioned so as to surround each reaction tube 35 constituting the reaction vessel 31 in the first portion 30A.

  The second heat exchanger 42B includes a heat medium supplied from the second heat source 41B, and each reaction tube 35 (and thus a dehydrogenation catalyst located in each reaction tube 35) constituting the reaction vessel 31 in the second portion 30B. 32) and the like. The second heat exchanger 42B has an inlet 43B and an outlet 44B, and is positioned so as to surround each reaction tube 35 constituting the reaction vessel 31 in the second portion 30B.

  Also in the dehydrogenation system 203 according to the present embodiment, the same effect as the dehydrogenation system 3 that improves the conversion rate while suppressing coking is produced.

[Third Embodiment]
Next, the dehydrogenation system 303 according to the third embodiment will be described. Below, a different point from the dehydrogenation system 3 which concerns on 1st Embodiment is demonstrated, and the overlapping description may be abbreviate | omitted.

  FIG. 4A is a block diagram showing a part of the dehydrogenation system 303 according to the third embodiment. As shown in FIG. 4A, the dehydrogenation system 303 is different from the dehydrogenation system 3 in that a reaction vessel 331B is adopted instead of the reaction vessel 31B (see FIG. 2). Other configurations of the dehydrogenation system 303 are the same as those described above with respect to the dehydrogenation system 3.

  The reaction vessel 331B is configured such that the raw material circulates inside. The reaction vessel 331B in the present embodiment includes a plurality of reaction tubes 35B arranged in parallel. In this embodiment, the average flow velocity of the fluid containing the raw material flowing through the reaction tube 35B constituting the reaction vessel 331B is larger than the average flow velocity of the fluid containing the raw material flowing through the reaction tube 35A constituting the reaction vessel 31A. In this way, the sum of the cross-sectional areas of all the reaction tubes 35B constituting the reaction vessel 331B is made smaller than the sum of the cross-sectional areas of all the reaction tubes 35A constituting the reaction vessel 31A. Here, the cross-sectional area means the area of a cross section perpendicular to the axial direction of each reaction tube 35A, 35B. Specifically, when the cross-sectional areas of each reaction tube 35A and each reaction tube 35B are substantially the same, the number of reaction tubes 35B constituting the reaction vessel 331B is set to the number of reaction tubes 35A constituting the reaction vessel 31A. Less than the number. The average flow rate is obtained by dividing the amount of fluid supplied per unit time to all reaction tubes constituting the reaction vessel by the sum of the cross-sectional areas of all reaction tubes constituting the reaction vessel. The calculated flow rate.

  Also in the dehydrogenation system 303 according to the present embodiment, the same effect as the dehydrogenation system 3 that improves the conversion rate while suppressing coking is produced. In the dehydrogenation system 303, the average flow velocity of the fluid flowing through the reaction tube 35B constituting the reaction vessel 331B is larger than the average flow velocity of the fluid flowing through the reaction tube 35A constituting the reaction vessel 31A. The thickness of the boundary film in the reaction tube 35B can be reduced (the volume of the boundary film is reduced). Since the boundary film is generally an area where coking is likely to occur, the dehydrogenation system 303 can further suppress coking. Therefore, in the dehydrogenation system 303, the reaction vessel 331B located in the second portion 30B can be set to a higher temperature or a lower pressure.

  In addition, as a structure which makes the average flow velocity of the fluid which distribute | circulates the inside of the reaction tube 35B which comprises the reaction container 331B larger than the average flow velocity of the fluid which distribute | circulates the inside of the reaction tube 35A which comprises the reaction container 31A, it is what was mentioned above. Instead, other configurations may be employed. For example, a configuration in which the diameter of each reaction tube 35B constituting the reaction vessel 331B is made smaller than the diameter of each reaction tube 35A constituting the reaction vessel 31A may be adopted. Good.

[Fourth Embodiment]
Next, the dehydrogenation system 403 according to the fourth embodiment will be described. Below, a different point from the dehydrogenation system 3 which concerns on 1st Embodiment is demonstrated, and the overlapping description may be abbreviate | omitted.

  FIG. 4B is a block diagram showing a part of the dehydrogenation system 403 according to the fourth embodiment. As shown in FIG. 4B, the dehydrogenation system 403 is different from the dehydrogenation system 3 in that a compressor 51 is employed instead of the pressure reducing valve 23 (see FIG. 2). Other configurations of the dehydrogenation system 403 are the same as those described above with respect to the dehydrogenation system 3.

  The compressor 51 has a function of adjusting the internal pressure of the reaction vessel 31B located in the second portion 30B to be higher than the internal pressure of the reaction vessel 31A located in the first portion 30A in the dehydrogenation reactor 30. In this embodiment, it is located in the communication pipe 38. The compressor 51 is connected to the control unit 24, and the driving thereof is controlled by the control unit 24.

  In the dehydrogenation system 403, when the dehydrogenation reaction product is generated by dehydrogenating MCH, the compressor 51 is driven by the control unit 24, and the second portion is connected to the second portion 30A via the communication pipe 38. The fluid flowing to the portion 30 </ b> B is pressurized by the compressor 51. Thereby, the pressure of the fluid flowing through each reaction tube 35B constituting the reaction vessel 31B is higher than the pressure of the fluid flowing through each reaction tube 35A constituting the reaction vessel 31A.

  Also in the dehydrogenation system 403 according to the present embodiment, the same effect as the dehydrogenation system 3 that improves the conversion rate while suppressing coking is produced. In the dehydrogenation system 403, the compressor 51 causes the pressure of the fluid flowing in each reaction tube 35B constituting the reaction vessel 31B to be higher than the pressure of the fluid flowing in each reaction tube 35A constituting the reaction vessel 31A. Therefore, the decomposition reaction from hydrocarbons to hydrogen and carbon can be made difficult to proceed in the reaction vessel 31B. Therefore, the dehydrogenation system 403 can further prevent coking in the reaction vessel 31B and can further suppress coking. In addition, as a structure which raises the pressure of the fluid which distribute | circulates each reaction tube 35B which comprises reaction container 31B, you may employ | adopt another structure instead of what was mentioned above.

[Fifth Embodiment]
Next, a dehydrogenation system 503 according to the fifth embodiment will be described. Below, a different point from the dehydrogenation system 3 which concerns on 1st Embodiment is demonstrated, and the overlapping description may be abbreviate | omitted.

  FIG. 5 is a block diagram showing a part of a dehydrogenation system 503 according to the fifth embodiment. As shown in FIG. 5, the dehydrogenation system 503 is different from the dehydrogenation system 3 in that it further includes a third portion 30C and a third heat exchanger 42C. Other configurations of the dehydrogenation system 503 are the same as those described above with respect to the dehydrogenation system 3.

  The third portion 30C is connected in parallel with the second portion 30B, and is located downstream of the first portion 30A in the raw material flow direction. The third portion 30C is configured in the same manner as the second portion 30B, and includes a reaction vessel 31B, a dehydrogenation catalyst 32B, a distribution unit 34B, and an aggregation unit 37B. The third heat exchanger 42C is configured similarly to the second heat exchanger 42B.

  The communication pipe 38 in this embodiment has a switching valve 61 on the downstream side of the pressure reducing valve 23 in the raw material flow direction. The switching valve 61 has a function of switching the flow of fluid between the second portion 30B and the third portion 30C, and examples thereof include a three-way valve. A branch pipe 62 is connected to the communication pipe 38 in the present embodiment. One end of the branch pipe 62 is connected to the communication pipe 38 via the switching valve 61, and the other end is connected to the distribution part 34B in the third portion 30C. Thereby, the fluid discharged | emitted from the aggregation part 37A of the 1st part 30A selectively distribute | circulates to either the 2nd part 30B or the 3rd part 30C.

  In this embodiment, the switching valve 63 is provided in the supply line of the heat medium heated in the second heat source 41B. The switching valve 63 has a function of switching the supply of the heat medium between the second portion 30B and the third portion 30C, and includes, for example, a three-way valve. Thus, the heat medium heated in the second heat source 41B is selectively supplied to either the second heat exchanger 42B or the third heat exchanger 42C via the switching valve 63.

  When the control unit 24 of the present embodiment operates using the second part 30B of the dehydrogenation reactor 30, the control part 24 controls the switching valve 61 so that the fluid flowing out from the first part 30A is second. The heat medium heated in the second heat source 41B is supplied to the inlet 43B of the second heat exchanger 42B located in the second part 30B by controlling the switching valve 63 while flowing through the part 30B. On the other hand, when the control unit 24 of the present embodiment operates using the third part 30C of the dehydrogenation reactor 30, the control part 24 controls the switching valve 61 so that the fluid that has flowed out from the first part 30A. The heat medium heated in the second heat source 41B is supplied to the inlet 43B of the third heat exchanger 42C located in the third part 30C by flowing through the third part 30C and controlling the switching valve 63.

  Also in the dehydrogenation system 503 according to the present embodiment, the same effect as the dehydrogenation system 3 that improves the conversion rate while suppressing coking is produced. Moreover, in the dehydrogenation system 503, since it becomes possible to switch and operate the second part 30B and the third part 30C of the dehydrogenation reactor 30, for example, in the reaction vessel 31B located in the second part 30B Even if the dehydrogenation catalyst 32B deteriorates to an extent that requires replacement, the dehydrogenation reaction can be continued by switching from the second portion 30B to the third portion 30C. Therefore, the dehydrogenation system 503 can maintain the production of hydrogen for a long time.

  The present invention is not limited to the above-described embodiment.

  For example, the configuration of the heat exchanger that heats the dehydrogenation reactor is not limited to that in the above-described embodiment. Further, the configuration of the dehydrogenation reactor is not limited to the multi-tube type as in the above embodiment, and a single-tube type may be adopted.

  For example, the same or different types of dehydrogenation catalyst 32A and dehydrogenation catalyst 32B may be employed. In particular, since the dehydrogenation catalyst 32B is used at a higher temperature than the dehydrogenation catalyst 32A, a sufficiently high reaction rate can be maintained even if the dehydrogenation reaction activity is relatively low. Is possible. Therefore, as the dehydrogenation catalyst 32A, from the viewpoint of suppressing coking, a catalyst having a smaller amount of noble metal than the dehydrogenation catalyst 32A is adopted, or from the viewpoint of suppressing the influence of poisonous substances, You may employ | adopt what adjusted activity with the poisonous substance.

  For example, when the temperature of the heat medium at the inlet 43A is adopted as the heating temperature of the heat medium at the first heat source 41A, the temperature of the heat medium at the inlet 43B as the temperature of the heat medium at the second heat source 41B. It is preferable to adopt the temperature of the corresponding part between the former stage and the latter stage.

  For example, off-gas discharged from the hydrogen purifier 6 (including hydrogen that could not be recovered as the purified gas) may be used as fuel for the heating mechanism without being supplied to the vaporizer 2.

  3,203,303,403,503 ... dehydrogenation system, 22,222 ... heating mechanism, 23 ... pressure reducing valve, 30,230 ... dehydrogenation reactor, 30A ... first part, 30B ... second part, 30C ... 3rd part, 31 ... Reaction vessel, 31A ... Reaction vessel (first vessel), 31B, 331B ... Reaction vessel (second vessel), 32, 32A, 32B ... Dehydrogenation catalyst, 41A ... First heat source, 41B ... 2nd heat source, 42A ... 1st heat exchanger (1st heating part), 42B ... 2nd heat exchanger (2nd heating part), 42C ... 3rd heat exchanger, 51 ... compressor.

Claims (5)

A dehydrogenation having a reaction vessel in which a raw material containing organic hydride circulates, and a dehydrogenation catalyst which is located in the reaction vessel and converts the organic hydride into hydrogen and a dehydrogenated product by a dehydrogenation reaction A reactor,
A heating unit for supplying heat to the dehydrogenation reactor,
The heating unit is
A first heating unit for heating the first part in the dehydrogenation reactor;
A second heating unit that heats the second part on the downstream side in the flow direction of the raw material from the first part in the dehydrogenation reactor,
The dehydrogenation system, wherein a heating temperature of the second heating unit is higher than a heating temperature of the first heating unit. The reaction container has a first container and a second container,
The first vessel is located in the first part of the dehydrogenation reactor;
The dehydrogenation system according to claim 1, wherein the second container is located in the second portion of the dehydrogenation reactor.   The average flow velocity of the fluid containing the raw material flowing through the inside of the reaction vessel located in the second portion is higher than the average flow velocity of the fluid containing the raw material flowing through the inside of the reaction vessel located in the first portion. The dehydrogenation system according to claim 1, wherein the dehydrogenation system is configured to be large.   The internal pressure of the reaction vessel located in the second part is configured to be lower than the internal pressure of the reaction vessel located in the first part. The dehydrogenation system described.   The internal pressure of the reaction vessel located in the second part is configured to be higher than the internal pressure of the reaction vessel located in the first part. The dehydrogenation system described.

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