JP2006221850A - Energy station - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an energy station capable of reducing the amount of the emission of CO<SB>2</SB>and efficiently supplying petroleum fuel, hydrogen, and electricity. <P>SOLUTION: In the energy station supplying petroleum fuel, high purity hydrogen, and electricity, a facility producing hydrogen by the dehydrogenation reaction of a hydride of aromatic hydrocarbon and a facility producing electricity and heat by operating a solid oxide fuel cell 6 with a reforming reaction product of the petroleum fuel are installed, and exhaust heat generated at the solid oxide fuel cell 6 is used as the heat source of the facility producing hydrogen by the dehydrogenation reaction of the hydride of the aromatic hydrocarbon. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to an energy station that supplies petroleum fuel, high-purity hydrogen, and electricity according to the customer's choice, and more particularly to an energy station that can efficiently supply high-purity hydrogen.

  In recent years, hydrogen has been considered promising as a new energy source due to environmental problems and energy problems. For example, development of hydrogen automobiles using hydrogen directly as fuel or fuel cells using hydrogen has been promoted. Although the fuel cell is small, it has high power generation efficiency. In addition, the fuel cell does not generate noise and vibration, and has excellent advantages such as use of exhaust heat.

  As for automobiles, fuel cell vehicles equipped with high-pressure hydrogen and hydrogen rotary engine vehicles are attracting attention as next-generation vehicles, and evaluations for practical applications such as public road tests are being conducted. On the other hand, it is expected that facilities such as hydrogen stations for supplying hydrogen as fuel to these vehicles will be required nationwide, and a method of transporting compressed hydrogen and liquid hydrogen and storing them in a hydrogen station, hydrogen A system that reforms methanol, city gas, and hydrocarbon petroleum fuel at a stand to produce and store hydrogen, a hydrogen factory that stores and transports hydrogen in aromatic hydrocarbons, and dehydrogenates it at a hydrogen stand. Various types of hydrogen stands such as a method for producing hydrogen have been proposed.

  However, the above method of transporting compressed hydrogen has low transport efficiency and requires a large space for installing a large cardle in the hydrogen stand, so it is not suitable for urban areas, and it is necessary to newly develop infrastructure. There is a problem that there is.

  In addition, although the method of transporting liquid hydrogen has high transport efficiency, there are problems that the production cost of liquid hydrogen is very high, and that boil-off and new infrastructure are required.

  Furthermore, in the method of producing hydrogen by city gas reforming, the city gas infrastructure is limited to urban areas, and there is a problem that the adoption of this method is not possible anywhere in the country. In addition, the method of producing hydrogen by methanol reforming has a problem that a new infrastructure is required.

  On the other hand, in the method of producing hydrogen by reforming hydrocarbon-based petroleum fuel and the method of producing hydrogen by storing and transporting hydrogen in aromatic hydrocarbons and dehydrogenating it in a hydrogen stand, Since the oil and fuel infrastructure can be used, the cost of infrastructure development can be minimized and the spread of hydrogen stations can be promoted. In particular, in the method using hydrides of aromatic hydrocarbons, the temperature of the dehydrogenation reactor in the hydrogen stand can be made lower than the temperature of the reforming reactor of petroleum fuel. It does not generate carbon dioxide, and can be recycled after hydrogen production. On the other hand, the dehydrogenation reaction of aromatic hydrocarbon hydride is an endothermic reaction, so the selection of the heat source of the dehydrogenation reactor is important to increase the energy efficiency. Several proposals have been made for this purpose. Has been made.

  For example, hydrogen is produced by a dehydrogenation reaction of an aromatic hydrocarbon hydride, and the resulting gas containing hydrogen is used to produce a solid oxide fuel cell, a molten carbonate fuel cell, an aqueous phosphoric acid fuel cell In a distributed power generation system that supplies power from a fuel cell, such as a method of using the exhaust heat of these fuel cells as a heat source for a dehydrogenation reaction, a part of the hydrogen generated in the dehydrogenation reactor, overflow from the fuel cell A method has been proposed in which a part of hydrogen and aromatic hydrocarbons and hydrides thereof are combusted by a combustor and the heat of combustion is used as a heat source for the dehydrogenation reaction (see Patent Document 1).

  In addition, in a high-pressure hydrogen supply system that supplies hydrogen produced by dehydrogenation of aromatic hydrocarbon hydride, a combustion turbine power generator using petroleum-based fuel such as kerosene or LPG as a fuel is operated. A method of using the obtained electric power and exhaust gas as a heat source for the dehydrogenation reaction has also been proposed (see Patent Document 2).

  On the other hand, it is considered that a long period of several decades or more is required to replace the conventional vehicle using petroleum fuel with the vehicle using hydrogen as fuel. During that period, the conventional petroleum fuel is used. There will be a mix of cars and cars that use hydrogen. In order to supply fuel to vehicles with different types of mixed fuel, installing hydrogen stations and oil fuel stations separately requires enormous costs and securing land. Thus, there is a demand for a mode in which the type of fuel can be selected at the station, and a conventional gas station having a function of supplying hydrogen has been proposed (see Patent Document 3).

  On the other hand, fuel cells that use hydrogen are also attracting attention as a distributed power source for households. For reforming hydrocarbons that can be supplied to homes, such as city gas, kerosene, and LPG, to operate the fuel cells. A method for obtaining hydrogen or a method for supplying hydrogen through a hydrogen pipeline has been proposed. However, in order to introduce new equipment into individual households, the cost burden of the household is large, so a method of generating electricity with medium and large scale fuel cells, converting it to electricity and heat and then supplying it to individual households is also proposed Has been. Here, in order to supply hydrogen to a medium-sized fuel cell, a hydrogen stand can be used, and electricity can be supplied regardless of the distance from the home.

  Based on the above, hydrogen supply facilities and fuel cells are installed in conventional oil fuel stations (automotive service stations), and three types of energy, petroleum-based fuel, hydrogen, and electricity, are supplied to meet customer demand. An energy station is desired. An energy station that can supply hydrocarbon fuel, hydrogen, and electricity by installing a reformer that uses petroleum fuel and other hydrocarbon fuels as raw materials for hydrogen production, and a fuel cell that uses the hydrogen-containing gas obtained from this. Has been proposed (see Patent Document 4).

JP 2004-39351 A JP 2004-197705 A JP 2002-241772 A JP 2002-337999 A

Under such circumstances, an object of the present invention is to provide an energy station that can reduce CO ₂ emissions and efficiently supply petroleum fuel, hydrogen, and electricity.

As a result of diligent research to solve this problem, the present inventor, as a method of adding a hydrogen supply function and an electric supply function to the function of a conventional petroleum fuel stand (automobile service station), the CO ₂ utilizing a dehydrogenation reactor aromatic hydrocarbon hydrides not discharged, by the supply of electricity utilizing fuel cells using modified products of petroleum fuels, the total energy station CO ₂ emissions In addition, a solid oxide fuel cell is used as a fuel cell, and its exhaust heat is used as a heat source for an aromatic hydrocarbon hydride dehydrogenation reactor. The present inventors have found that it is possible to increase the overall efficiency and completed the present invention. That is, the present invention relates to energy stations shown in 1 to 5 below.

1. In energy stations supplying petroleum fuel, high purity hydrogen and electricity,
Equipment for producing hydrogen by dehydrogenation of aromatic hydrocarbon hydride,
A facility for producing electricity and heat by operating a solid oxide fuel cell with the reforming reaction product of the petroleum fuel,
An energy station, wherein exhaust heat generated in the solid oxide fuel cell is used as a heat source of a facility for producing hydrogen by dehydrogenation of the hydride of the aromatic hydrocarbon.

2. A hydrogen refining facility is further provided in the latter stage of the facility for producing hydrogen by dehydrogenation of the aromatic hydrocarbon hydride, and obtained by dehydrogenation of the hydride of the aromatic hydrocarbon through the hydrogen refining facility. To a facility that produces high-purity hydrogen with a purity of 99.99% or more, supplies a part thereof as high-purity hydrogen, and produces another hydrogen by dehydrogenation of the aromatic hydrocarbon hydride. 2. The energy station according to 1 above, wherein the energy station is recycled.

3. 3. The energy station according to 1 or 2 above, wherein the dehydrogenation reactor of the facility for producing hydrogen by dehydrogenation of the aromatic hydrocarbon hydride is a fixed bed flow reactor.

4). The dehydrogenation catalyst used in the dehydrogenation reactor comprises at least one metal selected from the group consisting of platinum, ruthenium, palladium, rhodium, tin, rhenium, and germanium supported on a porous carrier, and has an average pore diameter 4. The energy station as described in 3 above, wherein is 40 to 130 mm.

5. 5. The energy station according to any one of 1 to 4, wherein the petroleum fuel used for operating the solid oxide fuel cell is gasoline, kerosene, naphtha, or LPG.

According to the energy station of the present invention, the combination of an aromatic hydrocarbon hydride dehydrogenation reactor and a fuel cell using a reformed product of petroleum fuel, while reducing CO ₂ emissions, Hydrogen and electricity can be supplied simultaneously, and a solid oxide fuel cell can be used as the fuel cell, and its exhaust heat can be used as a heat source for the dehydrogenation reactor, thereby improving the energy efficiency of the entire energy station. it can. In particular, if the energy station of the present invention is constructed using an existing petroleum fuel station, existing storage facilities and transportation facilities can be utilized, so that capital investment can be reduced, and conventional internal combustion engine vehicles can be reduced to fuel cell vehicles. Since the business can be continued for a long time during the transition period, there is a great practical advantage.

  Hereinafter, a preferred embodiment of the present invention will be specifically described with reference to FIG. However, the present invention is not limited to the form shown in FIG.

  The energy station shown in FIG. 1 includes a petroleum fuel tank 1, an aromatic hydrocarbon hydride tank 2, and a dehydrogenation reaction recovery oil tank 3. Here, the petroleum fuel tank 1 stores petroleum fuel to be supplied to the internal combustion engine automobile and the reformer 4, and the aromatic hydrocarbon hydride tank 2 is used to generate hydrogen by the dehydrogenation reactor 5. The aromatic hydrocarbon hydride is stored, and the dehydrogenation reaction recovery oil tank 3 stores recovered oil mainly composed of aromatic hydrocarbons generated after the dehydrogenation reaction. In addition, the aromatic hydrocarbon hydride tank 2 and the dehydrogenation reaction recovery oil tank 3 may be a two-chamber one tank whose interior is partitioned by a partition wall. The recovered oil recovered in the dehydrogenation reaction recovery oil tank 3 can be regenerated and reused by regenerating into a hydride of an aromatic hydrocarbon by a hydrogenation reaction.

  The energy station of the present invention is provided with a hydrogen supply function and an electric supply function while maintaining the function of a conventional oil fuel station (automobile service station), and can be received by a conventional oil fuel station. Services such as sales of kerosene, light oil, LPG, engine oil, etc., sales of car supplies such as tires, replacement of engine oil and tires, car washing, inspection work, etc. can be similarly received at the energy station of the present invention.

  In the energy station shown in FIG. 1, facilities for producing electricity and heat by operating a solid oxide fuel cell with a reforming reaction product of petroleum fuel include a reformer 4, a solid oxide fuel cell (SOFC). 6).

  The petroleum fuel supplied to the reformer 4 may be any of kerosene, light oil, and LPG sold at the energy station of the present invention in addition to gasoline. Moreover, as a petroleum fuel supplied to the reformer 4, what removed the sulfur content contained via a desulfurization apparatus is preferable. If there is a sulfur content in the petroleum fuel supplied to the reformer 4, the sulfur content becomes a poisoning substance for the reforming catalyst filled in the reformer 4. Is preferred. In addition, when using fuel without sulfur content, such as GTL, as petroleum fuel, it can use as it is.

The reformer 4 is an apparatus for obtaining a fuel containing hydrogen by a steam reforming reaction, a partial oxidation reaction, and an autothermal reforming reaction. When a polymer electrolyte fuel cell is used as a fuel cell, high-purity hydrogen is required. However, in the present invention, in view of utilization of exhaust heat to the dehydrogenation reactor 5, a solid oxide that operates even with relatively low-purity hydrogen. Type fuel cell 6 is used. Here, the hydrogen-containing fuel supplied to the solid oxide fuel cell 6 may contain methane, CO, CO _2, etc. in addition to hydrogen, but C2 or higher hydrocarbons cause coking. Since it is easy, it is preferable that it is not included.

  As the reforming catalyst used in the reformer 4, a catalyst generally known as a steam reforming catalyst may be used. A catalyst in which a metal such as Ni, Ru or Rh is supported on a carrier such as alumina, zirconia, or ceria. Used. The reforming reaction in the reformer 4 is preferably performed under the conditions of reaction temperature: 400 to 900 ° C., reaction pressure: normal pressure to 3 MPa, GHSV: 500 to 500,000, S / C: 0.5 to 3. .

  In order to supply electricity in the energy station, a generator using petroleum fuel other than the fuel cell as a raw material, for example, a gas turbine can be used. However, in the energy station of the present invention, the solid oxide fuel with high power generation efficiency is used. A battery 6 is used. The electricity generated by the solid oxide fuel cell 6 is provided to the community, and can be used in homes, buildings, offices, etc., or supplied to electric vehicles.

As a method for producing on-site high-purity hydrogen to be supplied to fuel cell vehicles, fuel cell buses, etc., there are conventional methods for reforming hydrocarbons such as petroleum fuel and city gas, or methanol. The produced gas contains CO and CO ₂ , and the hydrogen purity is at most 70 to 80%. Therefore, in order to obtain high-purity hydrogen (purity of 99.99% or more) for fuel cell vehicles, CO to be removed is used. After passing through a transformer and a CO removal device, it is necessary to further purify the product using ordinary hydrogen purification equipment such as PSA (pressure swing adsorption) and membrane separation. In contrast, according to the dehydrogenation reaction using the aromatic hydrocarbon hydride used in the present invention, there is no generation of CO or CO ₂ during the production of hydrogen, and the product gas contains unreacted aromatic carbon other than hydrogen. It contains only hydrogen hydride vapor, aromatic hydrocarbon vapor generated after the dehydrogenation reaction, and a small amount of methane produced by side reactions. These can be easily removed by gas-liquid separation or ordinary hydrogen purification equipment. Therefore, it is preferable as an on-site high-purity hydrogen production method from the viewpoint of simplification of equipment and cost reduction.

  In the energy station shown in FIG. 1, the facility for producing hydrogen by dehydrogenation of an aromatic hydrocarbon hydride includes an aromatic hydrocarbon hydride tank 2, a dehydrogenation reactor 5, and a recovered oil tank 3. However, the hydrogen production facility used in the energy station of the present invention may further include a hydrogen purification device, a gas-liquid separator, and the like. It is preferable that the aromatic hydrocarbon hydride as a raw material is pumped up from the aromatic hydrocarbon hydride tank 2 with a pump or the like, and supplied to the dehydrogenation reactor 5 after preheating.

  Examples of hydrides of aromatic hydrocarbons used in the present invention include cyclohexanes and decalins, but those having substituents are preferred from the viewpoint of safety and ease of handling of aromatic hydrocarbons generated after dehydrogenation reaction, It is preferable to use alkylcyclohexane such as methylcyclohexane, ethylcyclohexane, dimethylcyclohexane, diethylcyclohexane and trimethylcyclohexane, alkyldecalin such as methyldecalin, ethyldecalin, dimethyldecalin and diethyldecalin, and mixtures thereof.

  The dehydrogenation reactor 5 used in the present invention is filled with a catalyst, and an aromatic hydrocarbon hydride is supplied to cause a dehydrogenation reaction. Here, the supply method to the dehydrogenation reactor 5 can be either a method of supplying an aromatic hydrocarbon hydride as a liquid or a method of supplying it as a preheated gas. A system in which gas is supplied to the bed reactor is preferred.

  Further, the catalyst charged in the dehydrogenation reactor 5 is preferably a catalyst in which at least one metal selected from the group consisting of platinum, ruthenium, palladium, rhodium, tin, rhenium, and germanium is supported on a porous carrier. The average pore diameter is preferably selected as appropriate depending on the type of hydride of the aromatic hydrocarbon supplied to the dehydrogenation reactor 5. That is, a catalyst having an average pore diameter of 40 to 80 mm is particularly preferred when using one-ring cyclohexanes, and a catalyst having an average pore diameter of 65 to 130 mm is particularly preferred when using two-ring decalins. It is preferable to select them, and it is preferable that the volume of pores having a preferable pore diameter is 50% or more of the total pore volume.

In order to control the ratio of the average pore diameter and the pore volume of the catalyst, it is preferable to use Al ₂ O ₃ or SiO ₂ as the catalyst support, and each may be used alone or in an appropriate ratio. They may be used in combination. When the aromatic hydrocarbon hydride is a mixture of one ring and two rings, a catalyst having a preferable average pore diameter may be mixed and used depending on the composition.

  The metal loading of the catalyst is preferably in the range of 0.001 to 10% by mass, more preferably in the range of 0.01 to 5% by mass. If the metal loading is less than 0.001% by mass, the dehydrogenation reaction cannot be sufficiently progressed. On the other hand, even if the metal is loaded exceeding 10% by mass, an effect commensurate with the increase in the amount of metal cannot be obtained. .

  The dehydrogenation reaction carried out in the present invention is carried out in the presence of the above-mentioned catalyst for dehydrogenation reaction, LHSV: 0.5-4, reaction temperature: 100-450 ° C, preferably 250 ° C-450 ° C, reaction pressure: normal pressure-2MPa. Therefore, it is preferable to carry out the process while circulating hydrogen. Here, the hydrogen flow rate is preferably in the range of 0.01 to 10 in terms of a hydrogen / aromatic hydrocarbon hydride molar ratio. By conducting hydrogen dehydrogenation reaction, side reactions can be suppressed compared to when hydrogen is not circulated, and not only hydrogen can be produced efficiently, but also the oil recovered after dehydrogenation reaction is hydrogenated again. Thus, impurities contained in the reuse as an aromatic hydrocarbon hydride can be reduced. Furthermore, in order to produce hydrogen efficiently, it is preferable to select reaction conditions so that the conversion rate is 90% or more.

  Since the dehydrogenation reaction of the aromatic hydrocarbon hydride is an endothermic reaction, it is necessary to supply heat from the outside. However, in the energy station of the present invention, electricity is supplied as all or part of the heat source. The exhaust heat of the solid oxide fuel cell 6 used for the above is utilized. As a method of using the exhaust heat of the solid oxide fuel cell 6, for example, as shown in FIG. 2, a method in which exhaust gas is blown into the upper portion of the multi-tubular dehydrogenation reactor 5, or as shown in FIG. 3. A method of heating a hydride of an aromatic hydrocarbon via the heat exchanger 7, preferably a method of heating a hydride of an aromatic hydrocarbon and a mixture of hydrogen can be employed.

  The gas produced by the dehydrogenation reaction is mainly composed of hydrogen, but in addition, unreacted aromatic hydrocarbon hydrides, aromatic hydrocarbons produced by the dehydrogenation reaction, methane, ethane, etc. produced by side reactions. It may contain hydrocarbons, alkylcyclopentane generated by side reactions, and the like. However, carbon monoxide contained in the reaction product gas when hydrogen is produced by reforming reaction such as city gas, kerosene, naphtha, etc. is included in the dehydrogenation reaction product gas of hydrides of aromatic hydrocarbons. Absent.

  In order to supply the gas generated by the dehydrogenation reaction to the fuel cell vehicle, it is preferable to make the gas high purity hydrogen having a purity of 99.99% or more. It is preferable to further provide a hydrogen purification facility after the facility for producing hydrogen by hydride dehydrogenation. In addition, it is preferable to circulate hydrogen for the dehydrogenation reaction. However, if the purity of the circulated hydrogen is low, the advantage of performing the dehydrogenation reaction under the circulated hydrogen cannot be sufficiently obtained. It is preferable to recycle a part of high-purity hydrogen having a purity of 99.99% or more obtained through the process to a facility for producing hydrogen by dehydrogenation of hydrides of aromatic hydrocarbons. A preferred example of the energy station of the present invention equipped with a hydrogen purification facility is shown in FIGS.

  As the hydrogen purification equipment, apparatuses such as PSA (pressure swing adsorption), hydrogen separation membrane, etc., which are usually used for purifying hydrogen gas can be used. Here, when PSA is used as the hydrogen purification equipment, as shown in FIG. 4, the product gas from the dehydrogenation reactor 5 is sent to the gas-liquid separator 8 via the heat exchanger 7, and the gas-liquid separation is performed. It is preferable that the gas component and the oil component are separated by the vessel 8 and the obtained gas component is separated by the PSA 9 into high-purity hydrogen having a purity of 99.99% or more and hydrogen and other gases. When a hydrogen separation membrane is used as the hydrogen purification facility, as shown in FIG. 5, the product gas from the dehydrogenation reactor 5 is converted into high-purity hydrogen having a purity of 99.99% or more by the hydrogen separation membrane 10 and others. The other components are preferably sent to the gas-liquid separator 8 via the heat exchanger 7 and separated into hydrogen and other gases and oil by the gas-liquid separator 8. The gas-liquid separation may be either a pre-process or a post-process of the hydrogen purification process using the PSA 9 or the hydrogen separation membrane 10 or the like. However, when the hydrogen separation membrane 10 is used, the gas-liquid separation is performed after the hydrogen purification process. Preferably it is done. Moreover, in order to reduce the size of the entire facility, purification by the hydrogen separation membrane 10 is particularly preferable as gas purification. Here, examples of the hydrogen separation membrane include metal membranes, zeolite membranes, ceramic membranes, polymer membranes, etc., but it is possible to operate from components contained in the temperature, pressure, and fluid of the dehydrogenation reactor 5 as Pd alloys. It is preferable to use a film, and in particular, it is preferable to use a Pd—Cu film that can be thinned as a rolled film and has little hydrogen embrittlement.

  High-purity hydrogen having a purity of 99.99% or more produced through a hydrogen purifier is supplied to the fuel cell vehicle, but a part of it is recycled to the dehydrogenation reactor 5 and used as circulating hydrogen in the dehydrogenation reaction. It is preferable. The flowing hydrogen used for the dehydrogenation reaction is included in hydrogen introduced from the outside, hydrogen contained in the unpurified gas of the reaction product gas exiting from the dehydrogenation reactor 5, and gas not permeated through the hydrogen separation membrane 10. Hydrogen and hydrogen in the off-gas of PSA 9 can also be used. However, if the purity of hydrogen is low, the concentration of gas other than hydrogen becomes high during recycling, and the dehydrogenation reaction can be performed under hydrogen flow. Since a sufficient advantage cannot be obtained, it is particularly preferable to recycle high-purity hydrogen having a purity of 99.99% or more obtained through the hydrogen separation membrane 10 or obtained through the PSA 9.

  In the present invention, the gas recovered from the dehydrogenation reaction product gas after gas-liquid separation through a hydrogen purifier as low-purity hydrogen, or the low-purity hydrogen obtained by gas-liquid separation after passing through the hydrogen purifier is hydrogen and Since it contains lower hydrocarbons generated by side reactions and liquid vapor that could not be separated, these were burned with a burner together with other fuels to heat the dehydrogenation reactor 5, and so on. Can be used as a part.

  On the other hand, the oil recovered as a liquid through the two steps of the hydrogen purifier and the gas-liquid separation contains unreacted aromatic hydrocarbon hydride and aromatic hydrocarbon generated by the dehydrogenation reaction. These can be recovered and hydrogenated again to form an aromatic hydrocarbon hydride, which can be supplied again to the dehydrogenation reactor 5 for reuse.

It is a schematic diagram which shows the structure of the energy station of this invention. In the energy station of the present invention, the exhaust heat of the solid oxide fuel cell is used as a heat source of the dehydrogenation reactor. It is another example using the exhaust heat of a solid oxide fuel cell as a heat source of a dehydrogenation reactor in the energy station of this invention. It is a flowchart of the suitable example of the energy station of this invention, and is an example using PSA as a hydrogen purification apparatus. It is a flowchart of the other suitable example of the energy station of this invention, and is an example using a hydrogen separation membrane as a hydrogen purification apparatus.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Petroleum fuel tank 2 Aromatic hydrocarbon hydride tank 3 Dehydrogenation reaction recovery oil tank 4 Reformer 5 Dehydrogenation reactor 6 Solid oxide fuel cell (SOFC)
7 Heat exchanger 8 Gas-liquid separator 9 PSA (Pressure Swing Adsorption)
10 Hydrogen separation membrane

Claims (5)

In energy stations supplying petroleum fuel, high purity hydrogen and electricity,
Equipment for producing hydrogen by dehydrogenation of aromatic hydrocarbon hydride,
A facility for producing electricity and heat by operating a solid oxide fuel cell with the reforming reaction product of the petroleum fuel,
An energy station, wherein exhaust heat generated in the solid oxide fuel cell is used as a heat source of a facility for producing hydrogen by dehydrogenation of the hydride of the aromatic hydrocarbon.   A hydrogen refining facility is further provided in the latter stage of the facility for producing hydrogen by dehydrogenation of the aromatic hydrocarbon hydride, and obtained by dehydrogenation of the hydride of the aromatic hydrocarbon through the hydrogen refining facility. To a facility that produces high-purity hydrogen with a purity of 99.99% or more, supplies a part thereof as high-purity hydrogen, and produces another hydrogen by dehydrogenation of the aromatic hydrocarbon hydride. The energy station according to claim 1, wherein the energy station is recycled.   The energy station according to claim 1 or 2, wherein a dehydrogenation reactor of a facility for producing hydrogen by a dehydrogenation reaction of the hydride of the aromatic hydrocarbon is a fixed bed flow reactor.   The dehydrogenation catalyst used in the dehydrogenation reactor comprises at least one metal selected from the group consisting of platinum, ruthenium, palladium, rhodium, tin, rhenium, and germanium supported on a porous carrier, and has an average fine particle size. The energy station according to claim 3, wherein the hole diameter is 40 to 130 mm.   The energy station according to any one of claims 1 to 4, wherein the petroleum fuel used to operate the solid oxide fuel cell is gasoline, kerosene, naphtha, or LPG.

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