JP2003306303A - Hydrogen generator and hydrogen storage/supply apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a hydrogen generator which can avoid the increase in the size of its reaction apparatus due to a raw material supply means such as spray ejection. <P>SOLUTION: Hydrogen H is generated in a hydrogen generator 1 by the dehydrogenation of a hydrogenated derivative HA (for example, a saturated hydrocarbon) of an aromatic compound A (for example, an aromatic hydrocarbon) by contacting with a heated catalyst. The hydrogen generator 1 is equipped with a raw material storage part 14 to store the hydrogenated derivative HA and a catalyst bed 16 (for example, equipped with a communicating hole or the like) through which a hydrogen-containing gas can pass. <P>COPYRIGHT: (C)2004,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrogen generator for generating stored hydrogen by dehydrogenation of a hydrogenated derivative of an aromatic compound and a hydrogen storage / supply device using the hydrogen generator.

[0002]

2. Description of the Related Art In recent years, a fuel cell system using hydrogen gas has attracted attention as a clean energy source to replace fossil fuels. The generated hydrogen is temporarily stored, and the stored hydrogen is taken out again to be used as a fuel cell system. Various hydrogen storage / supply systems to be supplied to the are being investigated.

The Applicant has found that low cost, safety, transportability,
As a hydrogen storage / supply system with excellent storage capacity, aromatic compounds (unsaturated hydrocarbons) such as benzene and naphthalene are used as hydrogen storage, and hydrogenated products (saturated hydrocarbons) of these aromatic hydrocarbons are supplied as hydrogen. Hydrogen storage as a body
A supply system has already been applied (for example, Japanese Patent Application No. 200
1-69676 and others).

In such a hydrogen storage / supply system, a heated catalyst is used, and a saturated hydrocarbon (hydrogenated aromatic hydrocarbon) as a hydrogen supplier is sprayed onto the heated catalyst. It is supplied by injection.

[0005]

The reaction of extracting hydrogen from a saturated hydrocarbon (dehydrogenation reaction) is an endothermic reaction and requires a high temperature. Therefore, a reaction raw material (liquid) supplied by spray injection. Heat of vaporization (endothermic reaction)
It is difficult to maintain the catalyst temperature at a high temperature because it is necessary. For this reason, the supply amount of the reaction raw material supplied by spraying is limited, and in some cases, the raw material must be supplied intermittently.

Further, although the method of supplying the reaction raw material by spray injection contributes to the increase of reaction efficiency because the liquid film reaction can be utilized, the reaction is carried out only on the surface of the catalyst sprayed and sprayed. Many contributions to internal reactions could not be expected.

Further, in order to uniformly spray the spray toward the surface of the catalyst, it is necessary to secure a sufficient spray space in the reaction vessel, so that the reactor must be increased in size.

[0008] Therefore, an object of the present invention is to provide a hydrogen generator capable of avoiding an increase in the size of a reaction apparatus due to a raw material supply means such as spray injection.

[0009]

In order to solve the above-mentioned problems, the present invention involves contacting a hydrogenated derivative (eg, saturated hydrocarbon) of an aromatic compound (eg, aromatic hydrocarbon) with a heated catalyst. Is a hydrogen generator that produces hydrogen by dehydrogenation of a hydrogenated derivative.

This hydrogen generator comprises a raw material storage section for storing a hydrogenated derivative, a catalyst layer through which a gas containing hydrogen generated by the reaction can pass (for example, a communication hole is provided), and the raw material storage section. It is provided with a supply means for supplying the hydrogenated derivative to the catalyst layer by capillary action from the section.

According to such a hydrogen generator, the liquid hydrogenated derivative is stored in the raw material storage portion and is supplied to the catalyst layer by the supply means by the capillary phenomenon. When the hydrogenated derivative comes into contact with the heated catalyst in the catalyst layer, the hydrogenated derivative is instantaneously evaporated and the dehydrogenation reaction proceeds at the contact interface. The reaction product containing hydrogen gas generated by the reaction becomes a gas together with the unreacted hydrogenated derivative (unreacted raw material) and passes through the catalyst layer.

By passing the unreacted raw material in a gaseous state inside the catalyst layer, the dehydrogenation reaction also proceeds inside the catalyst layer. The reaction product passes through the catalyst layer, hydrogen gas is separated by any method, and hydrogen can be supplied.

As a result, the unreacted raw material at the contact interface becomes a vapor and a dehydrogenation reaction occurs even at the stage of passing through the catalyst layer, and the reaction occurs not only on the surface but also inside the catalyst layer. Is markedly increased.

According to such a hydrogen generator, since a means for supplying the raw material by spray injection or the like is not required,
It is possible to avoid increasing the size of the reactor.

If the catalyst layer is held via the heat insulating material, the heat of the catalyst layer is stored by the heat insulating material interposed between the catalyst layer heated to a high temperature and the raw material storing portion. Therefore, even if a raw material having a relatively low boiling point is used, it is possible to prevent the raw material from being heated and evaporated before it is brought into contact with the catalyst layer.

If the heating of this catalyst is electromagnetic induction heating,
The heating response becomes good, and the temperature control of the catalyst becomes easy.

Further, such a hydrogen generator is provided with a separating means for separating hydrogen from the reaction gas, and the hydrogen separated by the hydrogen separating means is hydrogenated with an aromatic compound to form a hydrogenated derivative. By using the hydrogen storage device as a hydrogen source of a hydrogen storage device that stores hydrogen, the hydrogen storage device can be used as a hydrogen storage / supply device that stores and / or supplies hydrogen.

[0018]

BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, embodiments of a hydrogen generator according to the present invention will be described in detail with reference to the drawings.

FIG. 1 is an explanatory view schematically showing the structure of a hydrogen generator 1 capable of supplying hydrogen.

This hydrogen generator mainly comprises a stock tank 2 as a raw material storage means for storing a hydrogenated derivative HA as a reaction raw material, and a reaction mixture H containing hydrogen by bringing a heated catalyst into contact with the reaction raw material. / A and a gas-liquid separator 4 as a separating means for separating hydrogen H from the reaction mixture H / A. The stock tank 2 and the reactor 3 are connected by a feed line 5. The reactor 3 and the gas-liquid separator 4 are connected by a feed line 6.

The gas-liquid separation device 4 cools the gaseous reaction mixture H / A and separates it into hydrogen gas H and liquid aromatic compound A, and a condenser (cooler) 41 and separated hydrogen. A hydrogen tank 4 for temporarily receiving the gas H and the aromatic compound A, and a hydrogen extraction unit 4 for recovering hydrogen gas (purified hydrogen gas) with high purity from the stock tank 42.
3 and 3. Also, from this gas-liquid separation device 4,
A discharge line 7 for discharging hydrogen gas as a reaction product and a discharge line 8 for discharging an aromatic compound A as a reaction product are connected.

The feed line 5 has a flow rate adjusting valve including a pump 9 for pressurizing and supplying the reaction raw material to the reaction apparatus 3 and a solenoid valve for adjusting the flow rate of the reaction raw material to be supplied to the reaction apparatus 3. Ten are arranged. In addition, the feed line 6 is provided with a flow rate adjusting valve 11 including an electromagnetic valve for adjusting the flow rate of the reaction product. As a result, the hydrogenated derivative HA stored in the stock tank 2 is connected to the reactor 3 through the feeder line 5, and the reaction mixture (mixed gas) H / A produced by the reactor 3 is connected.
Is fed from the reactor 3 to the gas-liquid separator 4.

These feed pump 9 and flow rate adjusting valve 1
Reference numerals 0 and 11 are connected to a control device 12 that controls the reaction by adjusting the reaction temperature in the reaction device 3 and the feed amount, reaction temperature, and the like in conjunction with an induction heating coil described later.

In the present invention, the hydrogenated derivative HA of the aromatic compound A is used as the reaction raw material. here,
Examples of the aromatic compound A include aromatic hydrocarbon compounds such as benzene, toluene, xylene, mesitylene, naphthalene, methylnaphthalene, anthracene, biphenyl, and phenanthrene, and alkyl derivatives thereof. Among them, benzene, toluene, xylene. , Naphthalene, etc. are particularly preferably used in terms of efficiency. The hydrogenated derivative HA of the aromatic compound A is a hydrogenated product of these aromatic compounds A. When the aromatic compound A is benzene, the hydrogenated derivative HA is a cyclohexane system, and When the group A compound is naphthalene, the hydrogenated derivative HA is a decalin / tetralin system.

The catalyst used in the present invention is a catalyst which produces hydrogen from a hydrogenated derivative HA by a dehydrogenation reaction,
A typical example is an active metal. Examples of such an active metal include nickel, palladium,
Precious metals such as platinum, rhodium, iridium, ruthenium, molybdenum, rhenium, tungsten, vanadium, osmium, chromium, cobalt, and iron can be used. These active metal catalysts may be used alone or in combination of two or more. Platinum, tungsten, rhenium, molybdenum, rhodium and vanadium are particularly preferable in terms of activity, stability, handleability and the like.

These active metals are used as a supported catalyst supported on a carrier. This supported catalyst may be of any type as long as it has voids through which a mixed product (mixed gas) H / A containing hydrogen gas as a reaction product can pass, and it may be in a granular form, a sheet form, a woven fabric form, A honeycomb shape, a mesh shape, a porous shape, or the like is appropriately selected according to the usage form. In any case, with the supported catalyst filled in the reaction vessel,
In the supported catalyst, it is necessary that a gas containing hydrogen gas as a reaction product generated by the reaction passes through the supported catalyst and is discharged. A sponge-like supported catalyst provided with open cells has a large surface area and is preferably exemplified. Further, a supported catalyst made of a honeycomb sheet material having upper and lower through holes is also exemplified as another example. Further, the catalyst layer may be a fluidized bed as long as it can be separated from the raw material reservoir.

As the carrier, for example, activated carbon, carbon nanotubes, molecular sieves, porous carriers such as zeolite, or known carriers such as silica gel and alumina can be used.

In this case, the supporting rate of the active metal on the carrier is
It is usually 0.1 to 50% by weight, preferably 0.
It is 5 to 20% by weight.

In the case of a composite metal catalyst in which two or more kinds of active metals are used in combination, the addition amount of the added metal M2 with respect to the main metal component M1 is 0.001 to 10, particularly preferably 0. It is preferably 01 to 5. Here, M1 is platinum, palladium, ruthenium, M2 is iridium, rhenium, nickel, molybdenum, tungsten,
Ruthenium, vanadium, osmium, chromium, cobalt and iron.

Examples of preferred supported catalysts include a carbon-supported platinum catalyst in which platinum, which is the main catalyst metal, is supported on carbon.
It is obtained by adding the above-mentioned carbonyl complex of active metal, acetylacetonate salt, cyclopentadienyl complex or the like at the same time or sequentially, and performing hydrogen reduction treatment after thermal decomposition.

As shown in FIG. 2, the reactor (reaction vessel) 3 is connected to a feed line 5 and a raw material inlet 13 for introducing a hydrogenated derivative HA as a reaction raw material, and the raw material inlet 13 is supplied. A raw material reservoir 14 that stores a liquid raw material (organic liquid raw material), and a catalyst layer 16 through a heat insulating material 15 around the periphery so as to withstand the stress of the raw material liquid surface stored in the raw material reservoir 14 Gas as a substance (hydrogen +
The gas storage part 17 which stores (organic gas) is provided. An exhaust port 18 is provided in the gas storage section 17, and the exhaust port 18 is connected to the feed line 6.

Further, the catalyst layer 16 is heated to a desired temperature by an appropriate means that does not impede the passage of gas in the catalyst layer 16. In the embodiment of the present invention, as shown in detail in FIG. 3, a heat dissipation pipe 19 is embedded. A heat medium capable of maintaining the catalyst at a desired temperature is circulated in the heat radiation pipe 19. As the heat medium, not only heat medium oil but also heating gas such as combustion gas may be used. Further, high temperature steam may be used depending on the conditions. Of course, an electric heater or the like may be incorporated. By selecting a material having good thermal conductivity for the catalyst layer 16, the heat radiated from the heat radiation pipe 19 can be efficiently transmitted to the catalyst.

As a modified example of heating using the heat radiating pipe 19, a heat exchanger having a space through which gas can pass is arranged on the catalyst layer 16 without burying the heat radiating pipe 19 in the catalyst layer 16. Then, the catalyst layer 16 may be heated by heat transfer from the heat exchanger.

A thermocouple (not shown) or the like may be inserted in the catalyst layer 16 to detect the temperature of the catalyst layer 16. As a result, the temperature of the catalyst is detected by the thermocouple, and the heat dissipation pipe 19
Control the temperature or circulation amount of the heat medium circulated in the
The temperature of the catalyst layer 16 can be controlled to the optimum temperature by adjusting the amount of the reaction raw material supplied to the reactor 3.

In the present invention, in order to perform heating more efficiently and with good response, as shown in FIG. 4, a spiral induction heating coil (electromagnetic induction coil) 19 'for heating the catalyst layer 16 instead of the heat radiation pipe 19 is used. Is preferably installed from inside or outside of the reactor 3 toward the catalyst layer 16.

The high frequency induction heating is for induction heating a conductor with a high frequency generated by passing a high frequency current through an electromagnetic induction coil. An eddy current is generated in the conductor due to the electromagnetic induction action, and the conductor is heated by Joule heat. Is overheated. The frequency of the high-frequency current applied to the electromagnetic induction coil is generally 350 to 450 kHz, although it depends on the impedance matching with the conductor to be heated.

Here, in order to efficiently heat the conductor to be heated, an object interposed between the electromagnetic induction coil and the conductor to be heated, such as a container for accommodating or fixing the catalyst layer or a heat insulating material, is used. It is preferable to use an insulator having high heat resistance such as alumina or ceramics.

As the shape of the electromagnetic induction coil, besides the general coil shape, a spiral shape can be adopted. In the case of the coil shape, the conductor to be heated is placed in the center of the coil, and in the case of the spiral shape, the conductor is placed on the center line of the spiral,
Can be heated efficiently and with good response.

In the case of performing high frequency induction heating, the temperature control is generally required because the conductor is continuously heated when the high frequency current is continuously supplied to the electromagnetic induction coil. As a method for controlling the temperature, various kinds of feedback control in which the temperature of the conductor is measured and the high-frequency current flowing in the electromagnetic induction coil is controlled are possible. For example, feedback control using a general thermocouple is sufficient. In addition, in order to balance the energy input for heating and the energy required for reaction, it is also possible to determine the amount of heat per unit time required for reaction and control the current (electric power) applied to the electromagnetic induction coil. It is possible.

In order to obtain the hydrogen amount of 18 l / min generally required in a fuel cell system using hydrogen by the dehydrogenation reaction from cyclohexane to benzene, 5 kW of electric energy is converted into thermal energy of about 1200 ca1 / s. Therefore, heat energy of 14.4 kca1 / min, that is, electric energy of 1 kW is required.

As a result, the temperature of the catalyst layer 16 is adjusted by appropriately adjusting the high frequency current to the induction heating coil 19 '. Since the metal-supported catalyst can be directly heated by high-frequency electromagnetic induction, the heat taken by the reaction can be quickly supplied, and the temperature adjustment becomes extremely easy. This allows
The temperature controllability of the catalyst layer is improved, and it becomes possible to continuously generate hydrogen. Moreover, if the temperature of the catalyst layer 16 is controlled to be constant, the amount of hydrogen generation can be freely increased or decreased by increasing or decreasing the amount of raw material supply.

When the induction heating coil 19 'is installed, care should be taken to prevent unnecessary portions from being heated by the induction heating coil 19'. This allows
For example, it is possible to avoid a temperature increase in a portion where heating is not preferable, including the raw material storage portion.

When the induction heating coil 19 'is used for heating, a conductor such as carbon is used as a carrier for the metal-supported catalyst, and is formed into a shape in which an eddy current is generated. This allows
The metal supported catalyst can be heated directly. Examples of the conductive carrier include a porous body made of metal such as carbon, activated carbon, graphite and Raney nickel, and a metal carbide such as molybdenum carbide, but other conductive bodies may be used. When the carrier is a non-conductor, conductivity may be imparted to the catalyst layer by forming a general conductor such as stainless steel in a layer with the carrier or using a carrier blended with a conductor.

In the embodiment of the present invention, the heat insulation as the supply means for supplying the liquid reaction raw material (organic liquid raw material) stored in the raw material storage portion 14 to the catalyst layer 16 by the capillarity under the catalyst layer 16. The felt 16a is provided. As the supply means, it is sufficient that the liquid raw material can be supplied to the catalyst layer 16 from the raw material storage portion 14 by the capillary phenomenon. It is preferable that the preferable supply means has a heat insulating property that blocks an increase in the temperature of the raw material storage portion 14 due to heat transfer or radiant heat from the catalyst layer 16.

As the supply means, it is preferable to use a fiber material having excellent heat resistance and chemical resistance at about 500 ° C., such as glass fiber and carbon fiber. All of these fibrous materials have low thermal conductivity, and by using a fibrous material in which fine fibers are hardened into a fiber bundle such as felt, woven cloth, non-woven cloth, or wool (wool), heat insulation is achieved. And a supply means having excellent suction properties.

The density (area weight) of these fibrous materials is
It is appropriately set in consideration of the degree of capillary phenomenon (wicking property). If the voids in the fibrous material are too wide, the capillary phenomenon will be less likely to occur, and if the fibrous material is too dense, the capillary phenomenon will be hindered and the amount of heat transfer to the raw material reservoir will increase.

When carbon felt is selected as the fiber material, one material can serve as the catalyst carrier and the heat insulating felt. Further, this carbon felt is also a material capable of induction heating, and the catalyst layer 16 can be heated by combining with the induction heating coil 19 '. In this case, the catalyst is supported above the carbon felt to form the catalyst layer 16, and the lower part serves as the supply means by the capillary phenomenon. By arranging the induction heating coil 19 ′ on the upper side, the catalyst layer 16 can be selectively heated and the temperature rise in the lower part of the supply means can be suppressed.

In the present invention, for example, when benzene is produced by the dehydrogenation reaction of cyclohexane, the catalyst is heated to a high temperature within the range of about 220 to 400 ° C. Considering the conversion efficiency of the dehydrogenation reaction, the temperature of this catalyst is preferably heated to 250 to 300 ° C. The catalyst temperature is set higher because the dehydrogenation reaction is an endothermic reaction and requires more heat energy.

If the reaction raw material is near the catalyst layer heated to 200 to 400 ° C., the reaction raw material may boil and evaporate. However, by interposing the adiabatic felt 16a, the catalyst layer The liquid raw material can be efficiently supplied to 16.

As the liquid raw material supplied to the catalyst layer 16 immediately evaporates and is subjected to the reaction, the liquid raw material can be continuously supplied to the catalyst layer continuously due to the capillary phenomenon.

Next, an example of a procedure for supplying hydrogen to the outside by the dehydrogenation reaction of cyclohexane using the hydrogen generator 1 equipped with the induction heating coil 19 'and the controller 12 will be briefly described with reference to FIG. To do.

The catalyst layer 16 of the reactor 3 is heated within the optimum temperature range of 250 to 300 ° C. Then,
The pump 9 is operated, the flow rate adjusting valve 10 is fully opened, and cyclohexane is supplied to the raw material reservoir 14. This raw material storage 1
Since the heat insulating material 15 is interposed between the catalyst layer 4 and the catalyst layer 16, heat conduction from the catalyst layer 16 is blocked and cyclohexane is prevented from evaporating. In addition, a heat insulating felt 16 is provided between the raw material reservoir 14 and the catalyst layer 16.
Since a is interposed, the radiant heat from the catalyst layer 16 is blocked, and cyclohexane (boiling point 81 ° C.) is prevented from evaporating.

When the liquid level rises by continuing to supply cyclohexane and the liquid level reaches the lower end of the adiabatic felt 16a, the adiabatic felt 16a absorbs cyclohexane by the capillary phenomenon and supplies the raw material to the catalyst layer 16, Contact the catalyst layer 16. As a result, cyclohexane evaporates, and at the same time, a dehydrogenation reaction occurs to generate benzene A and hydrogen H as reaction products. These products H / A are gases under the reaction atmosphere, and the reaction products H / A pass through the voids of the catalyst layer 16. The cyclohexene (unreacted raw material) that has evaporated without reacting at the contact interface contacts the catalyst in a gaseous state while passing through the catalyst layer 16 to further generate hydrogen.

The reaction product gas obtained by passing through the catalyst layer 16 reaches the gas storage portion 17, and then is sequentially sent from the outlet 18 through the feed line 6 to the gas-liquid separation device 4. It

In the gas-liquid separator 4, the benzene A is liquefied by being cooled by the condenser 41 and separated from the hydrogen gas H. Both the hydrogen gas H and the benzene A are temporarily stored in the stock tank 42, and the hydrogen gas H is discharged from the upper part of the stock tank 42, purified to the required purity in the hydrogen extraction part 43, and discharged from the discharge line 7. It Further, benzene A is discharged from the bottom of the stock tank 42.

In the preferred embodiment of the present invention, the pump 9, the flow rate adjusting and adjusting valves 10, 11, the thermocouple, and the induction heating coil 19 'are electrically connected to the control means 12, respectively, and based on the information of the thermocouple and the like. Further, by controlling the current applied to the induction heating coil 19 ', the operation of the pump 9 and the flow rate adjusting valves, etc., hydrogen can be generated more efficiently.

For example, the catalyst layer 1 is controlled by feeding back information on the thermocouple to control the current flowing through the induction heating coil 19 '.
The temperature of 6 is controlled to an appropriate temperature of 250 ° C. to 300 ° C. which is optimum. According to this structure, water can be continuously obtained by continuously supplying the raw materials. Further, by increasing / decreasing the feed amount of the raw material fed by the pump 9 and the flow rate adjusting valve 10, it is possible to easily increase / decrease the production amount of hydrogen.

Further, in the hydrogen generator 1 described above, since spray injection is not used, a space for spray injection is not required, and the volume of the reaction container can be reduced to downsize the device.

Although the hydrogen generator of the present invention has been described above, the hydrogen generator of the present invention can be used as a part of a hydrogen supply / storage system, or can be used by connecting it to a fuel cell using hydrogen gas as a raw material. May be. For example, hydrogen may be burned to generate steam, and a turbine may be rotated to generate electricity by a generator. Further, the electric power supply system of a conventional thermal power plant or nuclear power plant may be used in combination with the hydrogen generator of the present invention.

The embodiment of the present invention has been described in detail above with reference to the drawings. However, the specific configuration of the present invention is not limited to this embodiment, and the design can be changed without departing from the gist of the present invention. Etc. are included in the present invention.

[0061]

As described above, according to the present invention, it is practically possible to provide a hydrogen generator capable of avoiding an increase in the size of a reaction apparatus due to a raw material supply means such as spray injection. Exert a beneficial effect.

[Brief description of drawings]

FIG. 1 is an explanatory diagram schematically showing the configuration of a hydrogen generator according to an embodiment of the present invention.

FIG. 2 is an explanatory diagram schematically illustrating the configuration of the reaction device of FIG.

FIG. 3 is an explanatory diagram schematically illustrating the configuration of the heat dissipation pipe in FIG.

FIG. 4 is an explanatory diagram schematically illustrating a configuration of a modified example of the reaction device of FIG.

[Explanation of symbols]

1: Hydrogen generator 2: Stock tank 3: Reactor (reaction vessel) 4: Gas-liquid separation device 41: Condenser 42: Stock tank 43: Hydrogen extraction part 5: Feeding line 6: Feeding line 7: Discharge line 8: Discharge line 9: Pump 10: Flow control valve 11: Flow control valve 12: Control device 13: Raw material entrance 14: Raw material storage section 15: Insulation material 16: Catalyst layer 16a: Insulating felt 17: Gas storage section 18: outlet 19: Heat dissipation pipe 19 ': induction heating coil

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Claims (6)

[Claims] 1. A hydrogen generator for producing hydrogen by a dehydrogenation reaction of a hydrogenated derivative by bringing the hydrogenated derivative of an aromatic compound into contact with a heated catalyst, and a raw material storage section for storing the hydrogenated derivative, A catalyst layer disposed above the raw material storage part, through which a gas containing hydrogen generated by the reaction can pass, and a supply means for supplying a hydrogenated derivative from the raw material storage part to the catalyst layer by capillary action. A hydrogen generator characterized by being provided. 2. The hydrogen generator according to claim 1, wherein the supply means is a heat-resistant felt. 3. The hydrogen generator according to claim 2, wherein the catalyst layer and the heat-resistant felt are continuous with each other, and a catalyst layer is formed by supporting a catalyst on an upper portion of the heat-resistant felt. . 4. The hydrogen generator according to claim 1, wherein the catalyst layer is held via a heat insulating material. 5. The hydrogen generator according to claim 1, wherein the catalyst layer is heated by electromagnetic induction heating. 6. The hydrogen generator according to any one of claims 1 to 5, further comprising a separating means for separating hydrogen from the reaction gas, wherein a part or all of the hydrogen separated by the hydrogen separating means is aromatic. A hydrogen storage / supply device for storing and / or supplying hydrogen, which is used as a hydrogen source of a hydrogen storage device for storing hydrogen by hydrogenating a group compound into a hydrogenated derivative.