JP6194143B2 - Hydrogen and synthetic natural gas production apparatus and production method - Google Patents

Description

  The present invention relates to an apparatus and a method for producing hydrogen and synthetic natural gas.

  In recent years, the momentum for suppressing emission of carbon dioxide, which is a warming gas, has increased, and the use of hydrogen energy has been demanded. As a supply source of this hydrogen, a hydrogen supply chain using an organic chemical hydride method has attracted attention. In the organic chemical hydride method, hydrogen as a gas is chemically added to an aromatic compound by a hydrogenation reaction (hydrogenation reaction) of the aromatic compound to generate a hydrogenated aromatic compound (organic hydride). Since the hydrogenated aromatic compound is liquid at normal temperature and pressure, hydrogen can be stored and transported easily and safely. According to this approach, hydrogen is converted to hydrogenated aromatic compounds at the production site and transported in the form of hydrogenated aromatic compounds. And a hydrogenated aromatic compound produces | generates hydrogen and an aromatic compound by a dehydrogenation reaction in the plant, hydrogen station, etc. which are adjacent to hydrogen use places, such as a city. The aromatic compound produced by the dehydrogenation reaction is transported again to the hydrogen production site and used for the hydrogenation reaction.

  However, even when efficient transport of hydrogen energy as described above becomes possible, there are cases in which existing combustion equipment cannot be used because hydrogen has different combustion characteristics from hydrocarbon fuels. Therefore, when hydrogen energy becomes widespread, it may be necessary to introduce equipment that can use hydrogen. However, hydrogen can be converted into synthetic natural gas (substitute natural gas) mainly composed of methane by a methanation reaction with the recovered carbon dioxide. By converting hydrogen into synthetic natural gas in this way, hydrogen energy can be used even in existing equipment for fossil fuels.

  By the way, since the dehydrogenation reaction of the hydrogenated aromatic compound is an endothermic reaction, it is necessary to add heat from the outside. As a heat source for supplying this amount of heat, there is a dehydrogenation reactor that performs a dehydrogenation reaction with a power generation facility and an engine so that the exhaust gas discharged from the power generation facility and the dehydrogenation reactor can exchange heat ( For example, Patent Documents 1 and 2). If comprised in this way, the waste heat which a power generation equipment etc. generate | occur | produce can be used effectively, and the energy efficiency of the whole system including a hydrogen supply equipment, a power generation equipment, etc. can be improved.

JP2013-49601A JP 2010-77817 A

  The heat that can be used in the dehydrogenation reaction is not limited to the heat of combustion when the fuel is burned. For example, in a synthetic natural gas generator that generates synthetic natural gas from hydrogen and carbon dioxide by reverse shift reaction and methanation reaction, the methanation reaction is an exothermic reaction.

  In view of the above background, the present invention generates a synthetic natural gas from hydrogen and carbon dioxide by reverse shift reaction and methanation reaction, and generates hydrogen from a hydrogenated aromatic compound by dehydrogenation reaction. An object of the present invention is to improve thermal efficiency in an apparatus for producing hydrogen and synthetic natural gas having a hydrogen generator.

  In order to solve the above-mentioned problems, the present invention provides a hydrogen and synthetic natural gas production apparatus (1) for producing synthetic natural gas from hydrogen and carbon dioxide by reverse shift reaction and methanation reaction. It has a device (2) and a hydrogen generator (3) that generates hydrogen from a hydrogenated aromatic compound by a dehydrogenation reaction, and the reaction heat of the methanation reaction, which is an exothermic reaction, is converted into a dehydrogenation reaction, which is an endothermic reaction. Heat is supplied from the synthetic natural gas generator to the hydrogen generator so as to be used for the above.

  According to this configuration, the hydrogen generator can receive the amount of heat generated in the synthetic natural gas generator, and can perform a dehydrogenation reaction using this amount of heat. That is, most of the amount of heat necessary for the dehydrogenation reaction in the hydrogen generator can be covered by the amount of heat generated in the synthetic natural gas generator, and the amount of heat supplied from the outside can be greatly reduced. Thereby, the manufacturing apparatus of hydrogen and synthetic natural gas can reduce energy consumption and carbon dioxide emission. In addition, the apparatus for producing hydrogen and synthetic natural gas can reduce the carbon dioxide emission by burning the produced synthetic natural gas or hydrogen to cover the shortage of heat.

  In the above invention, the synthetic natural gas generator includes a high-temperature synthetic natural gas generator (11) that performs a reverse shift reaction and a methanation reaction at a high temperature, and a reverse shift at a lower temperature than the high-temperature synthetic natural gas generator. It is good to have a low-temperature synthetic natural gas production | generation apparatus (12) which performs reaction and methanation reaction.

  According to this configuration, the reaction rate and yield of the synthetic natural gas can be increased while increasing the heat recovery efficiency. Since the methanation reaction is an equilibrium reaction and an exothermic reaction, the yield of methane (synthetic natural gas) increases when the reaction conditions are lowered. However, when the reaction conditions are lowered, the reaction rate decreases and the amount of heat that can be recovered at a high temperature that can be used in the dehydrogenation reaction decreases. Since the operating temperature of the hydrogen generator is high, when the operating temperature of the synthetic natural gas generator is set to a low temperature, the hydrogen generator is efficiently heated to the operating temperature by the heat supplied from the synthetic natural gas generator. It becomes difficult to raise the temperature, and the temperature of the hydrogen generator needs to be raised again. Therefore, in the high-temperature SNG reactor, the reaction rate is increased by increasing the reaction conditions, and the amount of heat that can be recovered from the synthetic natural gas generator to the hydrogen generator is increased, thereby increasing the temperature of the hydrogen generator. Facilitate. On the other hand, in a low-temperature SNG reactor, by reducing the reaction conditions to a low temperature, it is possible to increase the yield of methane by setting the equilibrium to the product side (side where methane is generated). As described above, the apparatus for performing the reverse shift reaction and the methanation reaction is made into two stages of the high-temperature synthetic natural gas generator and the low-temperature synthetic natural gas generator, thereby providing heat supply to the hydrogen generator and synthetic natural gas. The yield can be improved at the same time.

  In the above invention, the high-temperature synthetic natural gas generator performs the reaction at a high temperature of 350 ° C. or higher and 500 ° C. or lower, and the low-temperature synthetic natural gas generator performs the reaction at a low temperature of 250 ° C. or higher and lower than 350 ° C. Good.

  According to this configuration, it is possible to increase the reaction rate and yield of the synthetic natural gas while increasing the heat recovery efficiency from the synthetic natural gas generator to the hydrogen generator.

  Another aspect of the present invention is a method for producing hydrogen and synthetic natural gas, comprising a synthetic natural gas production step of producing synthetic natural gas from hydrogen and carbon dioxide by a reverse shift reaction and a methanation reaction, and a dehydrogenation reaction. In the hydrogen generation step for generating hydrogen from the hydrogenated aromatic compound and the synthetic natural gas generation step, the reaction heat generated by the methanation reaction, which is an exothermic reaction, is supplied to the hydrogen generation step, and the dehydrogenation is an endothermic reaction. It is used for reaction.

  According to the above configuration, heat supply to the dehydrogenation reaction can be performed while suppressing the amount of carbon dioxide generated.

The block diagram which shows the hydrogen and synthetic natural gas manufacturing apparatus which concerns on embodiment

  Hereinafter, an embodiment of an energy supply system according to the present invention will be described with reference to the drawings. FIG. 1 is a block diagram showing the configuration of the energy supply system according to the first embodiment.

  As shown in FIG. 1, the hydrogen / synthetic natural gas production apparatus 1 performs heat exchange between the synthetic natural gas generation apparatus 2, the hydrogen generation apparatus 3, and the synthetic natural gas generation apparatus 2 and the hydrogen generation apparatus 3. It has the 1st heat exchange means 4 and the 2nd heat exchange means 5, and the heating apparatus 6 which supplies heat to a 1st heat exchange means. The hydrogen / synthetic natural gas production apparatus 1 receives supply of carbon dioxide, a hydrogenated aromatic compound (organic hydride), and hydrogen, and supplies hydrogen and synthetic natural gas to the outside. Note that the hydrogen / synthetic natural gas production apparatus 1 generates synthetic natural gas by using the hydrogen generated by the hydrogen generation apparatus 3 as a raw material when hydrogen is not supplied from the outside.

  The hydrogenated aromatic compound is a product of a hydrogenation reaction (hydrogenation reaction) of an aromatic compound, and may be any product as long as it is stable and dehydrogenated to become a stable aromatic compound. The aromatic compound is not particularly limited, but monocyclic aromatic compounds such as benzene, toluene and xylene, bicyclic aromatic compounds such as naphthalene, tetralin and methylnaphthalene, and tricyclic rings such as anthracene. These are aromatic compounds, and these can be used alone or as a mixture of two or more. The hydrogenated aromatic compound is obtained by hydrogenating the above aromatic compound, and a monocyclic hydrogenated aromatic compound such as cyclohexane, methylcyclohexane or dimethylcyclohexane, or a bicyclic ring such as tetralin, decalin or methyldecalin. Or a tricyclic hydrogenated aromatic compound such as tetradecahydroanthracene, which can be used alone or as a mixture of two or more. Hydrogenated aromatic compounds are liquids that are stable at room temperature and pressure. Of the above hydrogenated aromatic compounds and aromatic compounds, it is preferable to use methylcyclohexane as the hydrogenated aromatic compound and use toluene obtained by dehydrogenating methylcyclohexane as the aromatic compound.

  Synthetic natural gas (also referred to as SNG: Synthetic Natural Gas) is a gas synthesized to replace natural gas, and is mainly composed of methane.

  The synthetic natural gas generator 2 includes a high temperature SNG reactor 11, a low temperature SNG reactor 12, a first gas-liquid separator 13, and a methane separator 14. The hydrogen generator 3 includes an evaporator 21, a heater 22, a dehydrogenation reaction device 23, and a second gas / liquid separation device 24. The hydrogen / synthetic natural gas production apparatus 1 is configured as a plant.

  First, the synthetic natural gas generator 2 will be described. In the synthetic natural gas generator 2, the high temperature SNG reactor 11, the low temperature SNG reactor 12, the first gas-liquid separator 13, and the methane separator 14 are directly connected from the upstream side in the order described. Carbon dioxide and hydrogen as raw materials are mixed with each other and then supplied to the high temperature SNG reactor 11.

  The carbon dioxide as the raw material may be carbon dioxide in the air or carbon dioxide in exhaust gas generated by combustion of fuel in a generator or an internal combustion engine. The carbon dioxide in these air and exhaust gas is preferably separated from other components only by the carbon dioxide recovery device. The carbon dioxide separation device may be a device using a known carbon dioxide separation and recovery technique such as a chemical absorption method, a physical absorption method, or a membrane separation method. A carbon dioxide separator using a chemical absorption method uses, for example, an alkaline solution that selectively dissolves carbon dioxide as an absorbent. The carbon dioxide separator has an absorption part and a regeneration part. The absorption part and the regeneration part are each constituted by a container and are connected to each other through a pipe so as to be circulated. As the alkaline solution used as the absorbent, an alkanolamine or an aqueous potassium carbonate solution is used.

  In the absorption part, when the gas containing carbon dioxide and the absorbent are in alternating current contact, the carbon dioxide is dissolved in the absorbent from the gas, and the carbon dioxide is separated from the gas. The gas from which carbon dioxide has been separated is released from the absorber into the atmosphere. The absorbent that has absorbed the carbon dioxide is sent to the regeneration unit and undergoes a regeneration process. In the regeneration treatment, the absorbent that has absorbed carbon dioxide is heated, and the carbon dioxide is separated from the absorbent. In this way, carbon dioxide separated from other gases may be used as a raw material.

  Hydrogen as a raw material may be hydrogen supplied from the outside or hydrogen supplied from a hydrogen generator.

The high temperature SNG reactor 11 and the low temperature SNG reactor 12 perform a reverse shift reaction represented by the following formula (1) in the presence of a catalyst using carbon dioxide and hydrogen as raw materials, and carbon monoxide and water Is generated. The reaction represented by the formula (1) is an endothermic reaction of ΔH ₂₉₈ = 40.1 kJ / mol, and since the equilibrium is biased toward the side (right side) where carbon monoxide is generated as the temperature is higher, the reaction is performed at a higher temperature. Is advantageous. As the catalyst, a nickel-based catalyst is usually used.

The high-temperature SNG reactor 11 and the low-temperature SNG reactor 12 use hydrogen and carbon monoxide generated by the reverse shift reaction as raw materials, and are represented by the following formula (2) in the presence of a catalyst. Methane is produced by the Nation reaction. Similarly, a nickel-based catalyst is used as the catalyst.

The reaction represented by the formula (2) is an exothermic reaction with ΔH ₂₉₈ = −205.6 kJ / mol. In the methanation reaction, the number of moles decreases in the direction toward the right side. Therefore, from the viewpoint of chemical equilibrium, the lower the temperature and the higher the pressure, the easier the right direction. Since this reaction is an equilibrium reaction, the products include methane, hydrogen and carbon dioxide.

As described above, in the high-temperature SNG reactor 11 and the low-temperature SNG reactor 12, the reverse shift process for generating carbon monoxide from carbon dioxide and hydrogen by the reverse shift reaction, and the carbon dioxide and carbon monoxide by the methanation reaction. A methanation step of generating methane from at least one and hydrogen is performed. That is, the reaction of the following formula (3) is performed by adding the above formulas (1) and (2) and offsetting carbon monoxide. This reaction is an exothermic reaction of ΔH ₂₉₈ = −164.5 kJ / mol (= 40.1 + (− 205.6)). Therefore, in the high temperature SNG reactor 11 and the low temperature SNG reactor 12, heat is generated by the reaction. From the formula (3), in order to convert all the carbon dioxide into methane, the molar ratio of hydrogen to carbon dioxide is preferably 4, and may be 4 or more.

  In the high temperature SNG reaction apparatus 11, the temperature in the reaction apparatus is maintained at a high temperature of 350 ° C. or more and 500 ° C. or less. As described above, the higher the temperature, the easier the reaction in Formula (1) proceeds to the right, and the easier the reaction proceeds in Formula (2) to the left. Moreover, reaction temperature of each formula (1)-(2) becomes large, so that it is high temperature. In the high temperature SNG reactor 11, most of carbon dioxide is converted to carbon monoxide by reverse shift reaction, whereas the produced carbon monoxide is not completely converted to methane by methanation reaction, and carbon monoxide. A part of remains. Therefore, the products sent from the high temperature SNG reactor 11 to the low temperature SNG reactor 12 include carbon dioxide, hydrogen, carbon monoxide, and methane.

  In the low temperature SNG reactor 12, the temperature in the reactor is maintained at a low temperature of 250 ° C or higher and lower than 350 ° C. As described above, the lower the temperature, the slower the reaction rate. However, in Formula (1), the reaction easily proceeds to the left, and in Formula (2), the reaction easily proceeds to the right. Thereby, the components of the product sent from the low-temperature SNG reactor 12 to the first gas-liquid separator 13 are mainly methane, water, and hydrogen added excessively as a raw material.

  The reaction heat generated by the reaction in the high-temperature SNG reactor 11 is supplied to the heater 22 and the dehydrogenation reactor 23 via the first heat exchange means 4. That is, the 1st heat exchange means 4 absorbs the reaction heat of the high temperature SNG reaction apparatus 11, and the temperature of the reaction container of the high temperature SNG reaction apparatus 11 is maintained within a predetermined range.

  The reaction heat generated by the reaction in the low temperature SNG reactor 12 is supplied to the high temperature SNG reactor 11 and the evaporator 21 of the hydrogen generator 3 via the second heat exchange means 5 and used as preheating or evaporation heat. The That is, the 2nd heat exchange means 5 absorbs the reaction heat of the low temperature SNG reactor 12, and the temperature of the reaction container of the low temperature SNG reactor 12 is maintained within a predetermined range.

  The first gas-liquid separator 13 may be a known knockout drum. The product sent from the low-temperature SNG reactor 12 to the first gas-liquid separator 13 is cooled to 100 ° C. or lower by a cooling device (not shown), and water vapor is condensed into liquid water. In the first gas-liquid separator 13, the product gas containing methane and hydrogen as gases and the water as liquid are separated from each other, and the product gas is sent to the methane separator 14.

  The methane separator 14 separates methane from the product gas. The methane separation device 14 may be a known device using pressure swing adsorption (PSA) or a hydrogen separation membrane, and separates hydrogen and methane from the product gas containing methane and hydrogen. In the present embodiment, the methane separation device 14 is a pressure swing adsorption device. Methane from which hydrogen has been separated by the methane separation device 14 is supplied to the outside of the hydrogen / synthetic natural gas production device 1 as synthetic natural gas. The hydrogen separated by the methane separator 14 is mixed with carbon dioxide before being supplied into the high-temperature SNG reactor 11 in order to use it as the raw material hydrogen of the synthetic natural gas generator 2.

  Next, the hydrogen generator 3 will be described. In the hydrogen generator 3, the evaporator 21, the heater 22, the dehydrogenation reactor 23, and the second gas-liquid separator 24 are directly connected in the order described. The hydrogenated aromatic compound as a raw material is supplied as a liquid to the evaporator 21 and vaporized. The evaporator 21 vaporizes the hydrogenated aromatic compound using the heat supplied from the low-temperature SNG reactor 12 via the second heat exchange means 5. The vaporized hydrogenated aromatic compound is sent from the evaporator 21 to the heater 22 and heated. The heater 22 is disposed so as to be able to exchange heat with the high-temperature SNG reactor 11 via the first heat exchange means 4, and heats the vaporized hydrogenated aromatic compound to raise the temperature. For example, the first heat exchange unit 4 may generate high-temperature steam by using heat supplied from the high-temperature SNG reactor 11 and supply the steam to the heater 22.

The vaporized and heated hydrogenated aromatic compound is sent from the heater 22 to the dehydrogenation reactor 23. The dehydrogenation reactor 23 generates hydrogen and an aromatic compound from the hydrogenated aromatic compound by a dehydrogenation reaction in the presence of a catalyst. In the present embodiment, the dehydrogenation reactor 23 performs a dehydrogenation step of generating hydrogen and an aromatic compound from a hydrogenated aromatic compound by a dehydrogenation reaction. In this embodiment, a case where the hydrogenated aromatic compound is methylcyclohexane will be described. The dehydrogenation reaction of methylcyclohexane is represented by the following formula (4), and hydrogen and toluene are generated. The reaction represented by the formula (4) is an endothermic reaction of ΔH ₂₉₈ = 205.0 kJ / mol. The dehydrogenation reaction of other hydrogenated aromatic compounds is also an endothermic reaction.

The dehydrogenation reactor 23 is arranged so as to be able to exchange heat with the high-temperature SNG reactor 11 and the heating device 6 via the first heat exchange means 4 and is heated by the heat supplied from the high-temperature SNG reactor 11 and the heating device 6. . In the present embodiment, the heating device 6 supplies heat to the dehydrogenation reaction device 23 via the first heat exchange means 4, but in other embodiments, the dehydrogenation reaction device does not pass through the first heat exchange means 4. You may supply heat directly to 23. The heating device 6 may obtain combustion heat by burning the synthetic natural gas produced from the synthetic natural gas production device 2 or the hydrogen produced from the hydrogen production device 3, or fuel supplied from the outside. Combustion heat may be obtained by combustion. Although the structure of the dehydrogenation reaction apparatus 23 is not limited, A shell and tube type reaction apparatus can be applied. The dehydrogenation reactor 23 has a cylindrical shell and a plurality of tubes extending in the shell. The internal space of each tube is isolated from the internal space of the shell. Each tube is filled with a dehydrogenation catalyst that promotes the dehydrogenation reaction. The dehydrogenation catalyst may be, for example, a porous γ-alumina support on which at least one catalyst metal selected from platinum, palladium, rhodium, iridium, and ruthenium is supported. In particular, the surface area is 150 m ² / g or more, the pore volume is 0.40 cm ³ / g or more, the average pore diameter is 90 to 300 mm, and the proportion of pores with an average pore diameter of ± 30 mm relative to the total pore volume is 50%. A catalyst in which at least one catalyst metal selected from platinum, palladium, rhodium, iridium and ruthenium is supported on the porous γ-alumina support described above is desirable.

  Each tube of the dehydrogenation reactor 23 is supplied with a liquid hydrogenated aromatic compound and flows while contacting the catalyst. A high temperature fluid is supplied to the shell from the first heat exchanging means 4, heat exchange is performed with the tube, and the catalyst and the hydrogenated aromatic compound are heated. The high temperature fluid supplied from the first heat exchange means 4 is, for example, water vapor. The hydrogenated aromatic compound receives the amount of heat from the first heat exchange means 4 and generates hydrogen and an aromatic compound (toluene when the hydrogenated aromatic compound is methylcyclohexane) in the presence of the catalyst.

  The second gas-liquid separator 24 may be a known knockout drum. The product sent from the dehydrogenation reaction device 23 to the second gas-liquid separation device 24 is cooled by a cooling device (not shown), and the aromatic compound aggregates into a liquid. When the aromatic compound is toluene, the aromatic compound is cooled to 111 ° C. or lower, which is the boiling point of toluene. In the second gas-liquid separator 24, hydrogen as a gas and an aromatic compound as a liquid are separated from each other. Hydrogen is mixed with carbon dioxide before being supplied into the high-temperature SNG reactor 11, because part of it is used as a raw material for the synthetic natural gas generator 2. The remaining hydrogen is supplied to the outside of the hydrogen / synthetic natural gas production apparatus 1.

  The aromatic compound separated by the second gas-liquid separator 24 is transported to the aromatic compound hydrogenation facility by a ship, a pipeline, or the like, where the aromatic compound is hydrogenated, and again the hydrogenated aromatic compound. become. The generated hydrogenated aromatic compound is transported again by a ship, a pipeline, or the like, and supplied to the hydrogen generator 3 of the hydrogen / synthetic natural gas production apparatus 1. In this way, a hydrogen supply chain in which hydrogen is transported as a hydrogenated aromatic compound suitable for transport is constructed by circulating and transporting the aromatic compound and the hydrogenated aromatic compound.

  The hydrogen / synthetic natural gas production apparatus 1 configured as described above includes a hydrogen generation apparatus 3 for supplying hydrogen to the outside and a synthetic natural gas generation apparatus 2 for supplying synthetic natural gas to the outside. That is, the hydrogen / synthetic natural gas production apparatus 1 can supply hydrogen and synthetic natural gas to the outside. The hydrogen generator 3 receives the amount of heat generated in the synthetic natural gas generator 2 via the first heat exchange means 4 and the second heat exchange means 5, and performs a dehydrogenation reaction using this amount of heat. Therefore, most of the amount of heat necessary for the dehydrogenation reaction in the hydrogen generator 3 can be covered by the amount of heat generated from the synthetic natural gas generator 2, and the amount of heat to be supplied from the outside can be greatly reduced. Thereby, the energy usage amount and carbon dioxide emission amount of the hydrogen / synthetic natural gas production apparatus 1 can be reduced.

  In particular, since the synthetic natural gas generation device 2 is a device that generates synthetic natural gas using carbon dioxide as a raw material, the amount of carbon dioxide in the atmosphere can be reduced. Therefore, the hydrogen / synthetic natural gas production apparatus 1 according to the present embodiment can supply hydrogen, which is clean energy, and can reduce the amount of carbon dioxide generated in the production process. It is possible to reduce the carbon dioxide emitted from the apparatus by converting it into synthetic natural gas.

  In this embodiment, since the SNG reactor is divided into the high-temperature SNG reactor 11 and the low-temperature SNG reactor 12 in the synthetic natural gas generator 2, heat at a temperature suitable for the dehydrogenation reaction can be recovered. And the reaction rate and yield of synthetic natural gas can be increased. Since the methanation reaction represented by the above formula (2) is an equilibrium reaction and is an exothermic reaction, the yield of methane (synthetic natural gas) increases when the reaction conditions are lowered. However, when the reaction conditions are lowered, the reaction rate decreases and the amount of heat that can be supplied to the heater 22 and the dehydrogenation reaction device 23 via the first heat exchange means 4 decreases. In particular, since the dehydrogenation reactor 23 has a high operating temperature, when the operating temperatures of the high temperature SNG reactor 11 and the low temperature SNG reactor 12 are low, the dehydrogenation reactor 23 is efficiently brought to the operating temperature. It becomes difficult to raise the temperature, and the dehydrogenation reactor 23 needs to be raised again. Therefore, the high temperature SNG reactor 11 increases the reaction rate and the amount of heat that can be recovered by the first heat exchange means 4 by increasing the reaction conditions, while the low temperature SNG reactor 12 changes the reaction conditions. By lowering the temperature, the equilibrium can be made on the product side (the side on which methane is generated), and the yield of methane can be increased. That is, it is possible to achieve both an increase in the yield of synthetic natural gas in the synthetic natural gas generator 2 and an increase in the efficiency of heat supply to the dehydrogenation reactor 23.

  Although the description of the specific embodiment is finished as described above, the present invention is not limited to the above embodiment and can be widely modified. Various forms can be applied to the first heat exchange means 4 and the second heat exchange means 5. For example, the first heat exchange means 4 may be incorporated as a part of the high temperature SNG reactor 11, the heater 22, or the dehydrogenation reactor 23. For example, when the tube through which the reactants and products of the high-temperature SNG reactor 11 pass is provided so as to pass through the shell of the dehydrogenation reactor 23 and the heater 22, the tube is the first heat exchange means. 4 Further, the high-temperature SNG reaction apparatus 11 and the dehydrogenation reaction apparatus 23 are configured as one combined apparatus, and a structure that partitions the high-temperature SNG reaction apparatus 11 and the dehydrogenation reaction apparatus 23 is used as the first heat exchange means 4. Also good.

  DESCRIPTION OF SYMBOLS 1 ... Hydrogen and synthetic natural gas manufacturing apparatus, 2 ... Synthetic natural gas production | generation apparatus, 3 ... Hydrogen production apparatus, 4 ... 1st heat exchange means, 5 ... 2nd heat exchange means, 6 ... Heating apparatus, 11 ... High temperature SNG reaction Apparatus (high temperature synthesis natural gas production apparatus), 12 ... low temperature SNG reaction apparatus (low temperature synthesis natural gas production apparatus), 13 ... first gas-liquid separation apparatus, 14 ... methane separation apparatus, 21 ... evaporator, 22 ... heater, 23 ... Dehydrogenation reactor, 24 ... Second gas-liquid separator,

Claims (4)

An apparatus for producing hydrogen and synthetic natural gas,
A high-temperature synthetic natural gas generator that performs reverse shift reaction and methanation reaction at high temperature;
A low-temperature synthetic natural gas generator connected to a downstream side of the high-temperature synthetic natural gas generator, and performing a reverse shift reaction and a methanation reaction at a lower temperature than the high-temperature synthetic natural gas generator;
An evaporator that vaporizes the hydrogenated aromatic compound using heat supplied from the low-temperature synthetic natural gas generator;
The dehydration is connected to the downstream side of the evaporator and heated by the heat supplied from the high-temperature synthesis natural gas generator and generates hydrogen from the hydrogenated aromatic compound vaporized in the evaporator by a dehydrogenation reaction. An elementary reactor ,
Between the evaporator and the dehydrogenation reaction apparatus, a heater that is disposed so as to be capable of exchanging heat with the high-temperature synthetic natural gas generation apparatus and that heats the hydrogenated aromatic compound vaporized in the evaporator. An apparatus for producing hydrogen and synthetic natural gas. First heat exchange means for supplying reaction heat generated by the reaction in the high-temperature synthetic natural gas generator to the dehydrogenation reactor and the heater;
The apparatus for producing hydrogen and synthetic natural gas according to claim 1 , further comprising second heat exchange means for supplying reaction heat generated by the reaction in the low-temperature synthetic natural gas generating apparatus to the evaporator. . The apparatus for producing hydrogen and synthetic natural gas according to claim 2 , further comprising a heating device for supplying heat to the first heat exchange means. In the high-temperature synthetic natural gas generator, the reaction is performed at a high temperature of 350 ° C. or higher and 500 ° C. or lower,
The production of hydrogen and synthetic natural gas according to any one of claims 1 to 3 , wherein the low-temperature synthetic natural gas generator performs the reaction at a low temperature of 250 ° C or higher and lower than 350 ° C. apparatus.

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