JP2002053306A - Device for producing hydrogen and fuel cell system using the same - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a compact partial oxidation type hydrogen producing device capable of reducing the heat loss in a reformer, a heating furnace and a pipe line part for connecting both to each other, shortening a stating time and free from the leakage of a gas, and a fuel cell system using the device. SOLUTION: The heating furnace 25 is arranged in the outer peripheral part of the reformer 8, the heating furnace 24 is provided with a combustion part 23, an air heating pipe 32 and a fuel heating pipe 34 in the inner periphery side partitioned with a partition 41, a water vaporizing pipe 36 is provided in the outer periphery side of the partition 41, a U-turn passage of a combustion gas from the combustion part 32 is formed between the ceiling surface of the heating furnace and the partition 41, and the reformer 8 and the heating furnace 24 are formed into an integral structure. An outside box 30 is provided in the outer periphery of the integral structure, and air existing in an area surrounded with the outside box 30 and the integral structure of the reformer 8 and the heating furnace is charged as the air for combustion for the reformer 8 and the heating furnace 24. Because the raw materials for the reformer such as methane, air, water, and the like, are heated in the heating furnace and the length of the pipe line leading to the reformer 8 is minimized by forming the reformer 8 and the heating furnace 24 into the integral structure, thus the heat loss from the pipe line is reduced.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

[0001] The present invention relates to a partial oxidation hydrogen production apparatus for producing hydrogen by a reforming reaction using hydrocarbons as fuel, and a fuel cell system using the hydrogen production apparatus.

[0002]

2. Description of the Related Art Industrial uses of hydrogen are used for ammonia synthesis, methanol synthesis, hydrodesulfurization, etc.
Large external heat reformers that produce hydrogen of several thousand m ³ / h or more are widely used. In addition, as a small-scale industrial use of hydrogen, there is a use for the production of high-purity glass such as semiconductors and glass fibers, and in recent years, a small hydrogen production facility has attracted attention as a hydrogen source for fuel cells. .

[0003] The reaction for producing hydrogen will be briefly described below by using methane as a fuel. First, the following reaction is promoted by introducing methane and steam into the reaction tube. CH ₄ + H ₂ O → CO + 3H ₂ (a-1) CO + H ₂ O → CO ₂ + H ₂ (a-2) Here, the above reaction requires a high temperature of 600 to 900 ° C., and the reaction (a-1) Heat must be supplied continuously because of the endothermic reaction. This heat supply method is classified into an external heat method and an internal heat method (partial oxidation method). The external heating method is a method of heating from outside with an electric heater or a burner, and the internal heating method uses oxygen (or air) injected into a reaction tube and uses heat generated by the following oxidation reaction in the above reaction. Is the way. CH ₄ + 2O ₂ → CO ₂ + 2H ₂ O (a-3)

[0004] Next, a large amount of CO is generated by the above reaction, and this is converted into hydrogen by the following reaction using a device called a CO converter. CO + H ₂ O → CO ₂ + H ₂ (b-1) Generally, the reaction temperature of this CO converter is 250 to 3
The temperature is 50 ° C., and a copper-zinc-based catalyst which is a CO conversion catalyst is used to promote the above reaction.

Next, a system in which the reformer of the internal heat type shown in FIG. 3 and a polymer electrolyte fuel cell (PEFC) are combined will be described as an example. Table 1 shows the gas composition of each part of the system shown in FIG.

[0006]

[Table 1]

The system shown in FIG. 3 comprises a reformer 8, a first reformed gas cooler 10, a CO converter 12, a second reformed gas cooler 13, a CO selective oxidizer 15, a fuel cell 18, and a heating furnace 24. And so on.

Methane is supplied to the raw material supply pipe 5 of the reformer 8 from the methane supply pipe 1, air for partial oxidation is supplied from the air supply pipe 4, and steam is supplied from the steam supply pipe 3. The upper portion of the raw material supply pipe 5 of the reformer 8 is filled with a combustion catalyst layer 6 and a reforming catalyst layer 7. The air supplies 20% to 30% of the theoretical amount of air necessary for burning methane, and a part of methane is burned by the combustion catalyst layer 6, and the combustion reaction of the formula (a-3) occurs. This combustion reaction supplies reaction heat required for the reforming reaction of the formula (a-1). The gas exiting the combustion catalyst layer 6 enters the reforming catalyst layer 7,
At a reaction temperature of 600 to 900 ° C., the formula (a-1):
The reforming reaction (a-2) occurs to generate hydrogen. The reformed gas containing hydrogen is cooled to 250 to 350 ° C. in the first reformed gas cooler 10 and then the CO converter 1
Enter 2. The CO conversion catalyst 1 is provided in the CO converter 12.
1 and CO is converted to hydrogen by the reaction of the formula (b-1).

The reformed gas that has exited the CO converter 12 is cooled to 150 ° C.
It enters the selective oxidizer 15. Solid polymer fuel cell (PEF
In C), if CO is present in the fuel gas, the electrode is poisoned, and the power generation efficiency is greatly reduced. In order to prevent this, the CO concentration in the fuel gas needs to be 10 ppm or less. CO
The selective oxidizer 15 is filled with a CO selective oxidation catalyst 14, and by feeding a small amount of oxygen, the following reaction is selectively promoted to remove CO. CO + 1 / 2O ₂ → CO ₂ (c-1)

The reformed gas exiting the CO selective oxidizer 15 enters a fuel electrode (not shown) of the polymer electrolyte fuel cell 18 through a hydrogen supply pipe 16 and is supplied through an air supply pipe 17. Reacts with air to generate electricity. At this time, 70 to 90% of the hydrogen at the fuel electrode of the fuel cell 18 is used for power generation, and the remaining 30 to 10% of hydrogen is discharged from the unreacted hydrogen discharge pipe 20.

The unreacted hydrogen discharged from the unreacted hydrogen discharge pipe 20 is introduced into a heating furnace 24 and burned by a burner 23 together with methane and air supplied from a heating furnace methane supply pipe 21 and a heating furnace air supply pipe 22, respectively. Is done. The combustion heat is used as a heating source for methane, air, water, and the like to be charged into the reformer 8. At this time, the gas temperature in the heating furnace 24 is
About 600-900 ° C, depending on the amount of unreacted hydrogen
It is. In the heating furnace 24, the water in the water supply pipe 2 is heated,
It is supplied to the steam supply pipe 3. The combustion exhaust gas from the heating furnace 24 is discharged from the heating furnace gas extraction pipe 25 into the atmosphere.

[0012]

When hydrogen is generated by a high-temperature reforming reaction, if the thermal efficiency of the reformer 8 decreases,
The operating cost increases, and the economy of the reformer 8 decreases. In the case of the internal heat method, the heat dissipation from the device lowers the thermal efficiency, but it is necessary to increase the amount of air supplied to compensate for this. Therefore, nitrogen in the generated gas increases, which causes a decrease in hydrogen concentration. When the fuel cell 18 is used, the power generation efficiency is reduced due to a decrease in the hydrogen concentration. The total power generation efficiency of the fuel cell system is the product of the thermal efficiency of the reformer 8 and the power generation efficiency of the battery, and the improvement of the heat efficiency of the reformer 8 is an important factor in increasing the total power generation efficiency of the battery system. . In addition, a compact configuration is required due to problems such as the installation location of the reformer 8, and safety is an important issue particularly in the case of indoor installation.

In the reformer 8 of the prior art, the heat efficiency is not sufficiently considered, and a large amount of heat is released outside the system. That is, since the reformer 8 and the heating furnace 24 are independent facilities, each of which needs to maintain a high temperature of 600 ° C. to 900 ° C., it is necessary to thicken the heat insulating material to prevent heat loss.

However, when the reformer 8 is a small facility,
When the heat insulating material is made thicker, the area of the outer wall surface becomes significantly larger than that of the inner wall surface. Taking the reformer 8 that supplies hydrogen to a fuel cell equivalent to several kw as an example, the inner diameter of the reformer 8 body is 10
When the ordinary heat insulating material is installed on the outer periphery of the reformer 8, the diameter becomes about 200 mm, the area ratio of the outer wall surface to the inner wall surface is three times, and the heat loss is about three times. And the volume of the device is 9 times. This tendency becomes remarkable as the equipment becomes smaller. Therefore, the thermal efficiency of the entire reformer 8 and the heating furnace 24 has been reduced.

Further, in the above-mentioned prior art, the steam generated in the heating furnace 24 is sent to the reformer 8 through the pipe 3. Particularly, in the case of a small-sized apparatus, since the pipe 3 is thin, a heat insulating material is wound. Also, there is a problem that heat loss due to an increase in the outer wall surface of the heat insulating material increases, and a large amount of heat loss occurs in the pipe 3. Further, when heat loss occurs in the pipe 3, the pipe 3
There are also problems such as the generation of drain inside.

Further, in the conventional structure, a large number of high-temperature pipes for supplying fuel, air and the like to the reformer 8 and the heating furnace 24 are required, which has the same problem.

The reformer 8 uses a reforming catalyst to reform hydrocarbons such as methane with steam to produce hydrogen. However, since the reforming catalyst has a large heat capacity, the temperature required for the reforming reaction ( 6
A long start-up time is required to raise the temperature to 00 to 900 ° C.). In particular, when a small fuel cell system for home use is targeted, a rapid start-up may be required due to a sudden load change or a night stop state.

Further, in the heating furnace 24, generation of CO and the like due to incomplete combustion and leakage thereof become a problem. Even if a gas detector such as hydrogen or CO is used as a countermeasure against these gas leaks, it is difficult to completely detect gas leaks from the entire surface of the reformer 8. Further, the reformer 8 and the heating furnace 24 must be completely sealed by welding or the like in order to prevent gas leakage.

In the reformer 8 and the heating furnace 24, gas leakage from the apparatus poses a serious safety problem. The gas generated from the reformer 8 contains flammable gases such as hydrogen, methane and CO. Among them, CO is particularly toxic, and a small amount of leakage to the outside is also dangerous. This is an important issue.

An object of the present invention is to provide a partially oxidizing hydrogen production apparatus which is compact, has a short start-up time, and has no gas leakage, reducing heat loss in a reformer, a heating furnace, and a piping section connecting the two. An object of the present invention is to provide a fuel cell system provided with the hydrogen production device.

[0021]

The object of the present invention is to provide an L
In a hydrogen production apparatus having a reformer that generates a hydrogen-rich gas by a reforming reaction between a hydrocarbon-based fuel such as NG, LPG, naphtha, and kerosene and a gas rich in oxygen and water, an outer peripheral portion of the reformer The problem is solved by a hydrogen production apparatus provided with a heating furnace for heating hydrocarbon fuel, oxygen-rich gas and water.

In the hydrogen production apparatus of the present invention, the reformer and the heating furnace disposed on the outer periphery thereof are housed in an outer box, and the outer box, the reformer, and the heater are integrally formed. It is preferable to provide a structure in which a space portion is provided between the first and second portions, and a flow path for introducing gas present in the space portion to the combustion air supply portion of the reformer and the heating furnace is provided.

In the heating furnace, a combustion section, an air heating pipe and a fuel heating pipe are arranged on an inner peripheral side partitioned by a partition having an open top, and a water evaporating pipe is provided on an outer peripheral side partitioned by the partition. And a combustion gas outlet at the bottom of the outer wall of the heating furnace,
It is preferable that a U-turn path for the combustion gas from the combustion section is formed between the ceiling surface of the heating furnace and the partition wall.

Further, a gas detector is arranged in the outer box,
A configuration in which a thermometer is arranged in the heating furnace to detect gas leakage from the reformer or the heating furnace and the alarm device is activated.

Further, a flow path for introducing the reformed gas obtained by the hydrogen production apparatus of the present invention via a CO selective oxidizer into a fuel cell and a gas containing unreacted hydrogen discharged from the fuel cell are subjected to hydrogen production. A fuel cell system provided with a flow path for circulating and supplying the heating furnace of the apparatus is also within the scope of the present invention.

[0026]

The operating temperature of the heating furnace is the operating temperature of the reformer.
Since the temperature is close to 00 to 900 ° C., heat loss from the reformer to the outside can be almost prevented by installing a heating furnace around the reformer.

That is, since the reaction temperature of the reformer and the combustion temperature in the heating furnace are almost equal, the heat loss from the reformer can be eliminated by providing the heating furnace on the outer periphery of the reformer. The heat insulator for the reformer is not required.

Further, by forming the reformer and the heating furnace into an integrated structure, the heating furnace heats the raw materials for the reformer such as methane, air, and water, and minimizes the length of a pipe leading to the reformer. And the heat loss from this pipe can be reduced.

Further, the heating furnace of the present invention has a double structure separated by a partition wall, a burner is installed in an inner room, and a structure in which combustion gas from the burner is reversed from the inside of the partition wall to the outside thereof is provided. Air heating pipe, fuel heating pipe,
By installing the water evaporation pipe (water heating pipe), the temperature of the combustion gas sequentially decreases in accordance with the flow direction of the combustion gas. Therefore, the temperature of the inside partitioned by the partition of the heating furnace, that is, the temperature of the portion in contact with the reformer is high, and the temperature of the gas outside the partition partitioned by the partition is reduced to 300 to 400 ° C. Heat loss can be reduced.

Further, by providing a space for preheating the reformer and the air to be supplied to the heating furnace between the outer box of the heating furnace and the outer box, the heat dissipated from the outer periphery of the heater can be reduced. Can be taken into the system as a heat source of the air introduced into the system, and the overall heat loss can be kept low.

Generally, the starting of the reformer requires a long time to raise the temperature because the heat capacity of the reforming catalyst is large, but the heating furnace can be started up quickly because there is no medium having a large heat capacity.
Therefore, by installing a heating furnace around the outer periphery of the reformer, the heating furnace quickly rises and becomes hot. Since the heating furnace heats the reformer having a low temperature rising rate in this manner, the temperature rising rate of the reformer can be increased, and the startup time can be shortened.

In the hydrogen production apparatus of the present invention, a heating furnace is disposed on the outer periphery of the reformer, and the heating furnace is entirely covered with an outer box. Therefore, the flammable gas or toxic gas leaked from the reformer or the heating furnace is mixed with the combustion air in the outer box, sucked and used in the reformer and the heating furnace, and leaks from the outer box to the outside. Never.

Further, the flammable gas and toxic gas leaked from the reformer or the heating furnace are collected inside the outer box and sucked into the combustion air blower. Therefore, by detecting flammable gas and toxic gas at the inlet of the blower, gas leakage from any location can be detected. Further, when gas leaks out of the reformer, the combustible gas is mixed into the combustion air, so that the temperature of the heating furnace increases. Therefore, by measuring the temperature in the heating furnace, it is possible to easily detect a gas leak, and it is possible to automatically stop safely.

In order to prevent the gas leaked from the reformer or the like from leaking out of the system by the above method, it is not necessary to provide an expensive welding structure especially in the heating furnace. Therefore, since the outer box and the like can be manufactured by press working or the like, an economical apparatus can be realized by using an inexpensive metal thin plate for the outer box.

[0035]

DESCRIPTION OF THE PREFERRED EMBODIMENTS A hydrogen production apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 1A is a perspective view of a hydrogen production apparatus structure (without the outer box 30) in which a heating furnace 24 is installed on the outer periphery of the reformer 8, and FIG. FIG. 3 is a horizontal cross-sectional view of the upper end when an outer box 30 covering the heating furnace 24 is installed. FIG. 1C shows a longitudinal sectional view of the hydrogen production apparatus. FIG. 2 shows a system in which the hydrogen production apparatus (reformer) shown in FIG. 1 and a fuel cell are combined. Here, the external structures of the reformer 8 and the heating furnace 24 are shown in a square shape, but they may be formed in a polygonal or round shape.

Inside the reformer 8, methane required for the reforming reaction provided at the bottom is supplied from a methane supply pipe 1, and water is supplied from a water supply pipe 2. Further, air or a gas rich in oxygen (hereinafter, air is used as the gas) to burn a part of methane and give reaction heat necessary for the reforming reaction is simultaneously supplied to the air supply pipe 4.
(FIG. 2). The air supplied from the air supply pipe 4 is slightly warmed in the space between the outer furnace 30 surrounding the reformer 8 and the heating furnace 24 and the heating furnace 24 and supplied to the reformer 8 by the blower 40. Supply.

A burner 23 is attached to the bottom of the heating furnace 24. The burner 23 supplies unreacted hydrogen from an unreacted hydrogen discharge pipe 20 at the outlet of the fuel cell 18 and fuel methane as required. The fuel is burned by the air heated in the heated air supply pipe 33. Methane supplied from the methane supply pipe 1 is supplied to the methane heating pipe 34 in the heating furnace 24 for 300 to 5 methane.
It is heated to 00 ° C., passed through a heated methane supply pipe 35, and led to the raw material supply device 5 in the reformer 8. The water supplied from the water supply pipe 2 is sent to a water evaporation pipe 36 in the heating furnace 24, and is heated and evaporated in the water evaporation pipe 36. The water vapor extracted from the water evaporation pipe 36 passes through a saturated steam supply pipe 37 and enters a steam heating pipe 39.

As will be described later, a reformed gas of 600 to 900 ° C. is generated on the reforming catalyst layer 7 in the reformer 8, and this gas is supplied to the CO conversion layer disposed above the reforming catalyst layer 7. The CO is sent to the catalyst layer 11, and CO is obtained as CO ₂ and hydrogen according to the reaction of the formula (b-1).
° C, it is necessary to lower the temperature of the reformed gas to this temperature. Therefore, the saturated steam is supplied by the steam heating pipe 39 disposed between the reforming catalyst layer 7 and the CO shift catalyst layer 11 to 300 steam.
~ 500 ° C heated steam and reformed gas at 20
Cool to 0-350 ° C. The steam taken out from the steam heating pipe 39 passes through the heating steam extraction pipe 38 and is guided to the heating furnace 24, and is supplied from the steam supply pipe 3 at the bottom of the heating furnace 24 to the raw material supply device 5 installed at the bottom of the reformer 8. Supplied to

Usually, the reformer 8 and the heating furnace 24 are installed independently. In this case, the methane, steam, air or oxygen-rich gas preheated in the heating furnace 24 is preheated, Since the pipes are piped under a low-temperature atmospheric environment until they are sent to the feed pipe 8, it is necessary to cover these supply pipes with a heat insulating material. Therefore, there is a problem that the preheating gas is cooled. In particular, in the case of a small-sized device, the pipe becomes thinner, so that the heat loss increases. However, by integrating the reformer 8 and the heating furnace 24 as in the present invention, this problem can be solved.

In the feeder 5, methane, steam and air are mixed and enter the combustion catalyst layer 6 in the reformer 8. Since the methane concentration in the source gas is low, gas phase combustion cannot be performed as it is. For this reason, a catalytic combustion method is employed, but the combustion catalyst layer 6 generates a high-temperature gas necessary for the reforming reaction by the reaction between methane and air shown in the equation (a-3). This high-temperature gas is at 800 to 1000 ° C. and enters the reforming catalyst layer 7 disposed above the combustion catalyst layer 6. In the reforming catalyst layer 7, the formulas (a-1) and (a-2)
A reforming reaction occurs to generate a hydrogen-rich gas. Since the reforming reaction is an endothermic reaction, the temperature of the reformed gas at the outlet of the reforming catalyst layer 7 is about 600 to 900 ° C., and the steam superheater 39 is heated by this gas. Conversely, the reformed gas is cooled to 200 to 350 ° C. and enters the CO conversion catalyst layer 11. Here, the reaction of the formula (b-1) in which CO is converted to hydrogen occurs, the hydrogen concentration is increased, and the reformed gas is taken out of the system from the reformed gas take-out pipe 9.

The heating furnace 24 is provided with a partition wall 41 which stands vertically from the bottom thereof.
4 is almost bisected. Upper end of partition 41 and heating furnace 2
A space for gas distribution is provided between the ceiling and the ceiling wall of No. 4. The burner 23 is disposed at the bottom of the space inside the heating furnace 24 partitioned by the partition 41, and the air heating pipe 3 is disposed above the burner 23.
2 and a methane heating pipe 34 are arranged, a water evaporating pipe 36 is arranged in a space outside the heating furnace 24 partitioned by the partition 41, and a heating furnace gas extraction pipe 25 is provided by the outer heating furnace partitioned by the partition 41. Connected to bottom wall.

The combustion gas burned by the burner 23 is burner 2
The air is cooled by an air heating pipe 32, a methane heating pipe 34, and a water evaporating pipe 36, which are sequentially disposed above the heating furnace 3, and is taken out of a combustion furnace gas extraction pipe 25 disposed at the bottom of the heating furnace 24 to the outside. Therefore, the rising portion of the combustion gas in the heating furnace 24 adjacent to the reformer 8 is under a high temperature condition,
Since the temperature of the outer wall of the adjacent reformer 8 is substantially equal to that of the adjacent reformer 8, the heat dissipated from the reformer 8 is not generated. Further, in a region where the rising combustion gas is reversed and becomes a downward flow, a plurality of water evaporation pipes 36 are provided, so that the temperature of the combustion gas decreases, and
° C, and the temperature at which the combustion gas is discharged from the combustion gas extraction pipe 25 drops to about 100 to 150 ° C. Therefore, the temperature of the outer wall of the heating furnace 24 is lower than that of the reformer 8 and the like, so that heat dissipation from the outer wall of the heating furnace 24 can be suppressed. Further, the combustion air used in the heating furnace 24 and the reformer 8 is introduced into the outer box from the air inlet 31, and is heated between the heating furnace 24 and the outer box 30 by the heat radiated from the heating furnace 24.

Therefore, the amount of heat dissipated from the outer box 30 to the outside of the system is extremely small, and the amount of heat dissipated can be reduced. In particular, a small device has a great effect of reducing the amount of heat dissipated.

Although the heating furnace 24 has a small heat capacity and a short heating time, the reformer 8 needs a long heating time because it is filled with a catalyst.
By integrating the reformer 4 and the reformer 8, the reformer 8 can be heated by the heating furnace 24 when the hydrogen production apparatus is started, so that the start-up time of the reformer 8 can be shortened.

Since leakage of hydrogen and CO from the reformer 8 and CO and the like due to incomplete combustion from the heating furnace 24 to the outside of the apparatus is highly dangerous, even a small amount of leakage is detected and the apparatus is stopped safely. There is a need to. Should any of these gases leak, the leaked gas will remain in the heating furnace 24 and the outer box 30 surrounding it.
Therefore, a detector (not shown) for detecting these gases is provided at the inlet of the gas suction blower 40 or by a thermometer (not shown) provided in the heating furnace 24. By detecting an increase in the furnace temperature, predicting the occurrence of the gas leakage and activating an alarm device (not shown) to stop the device, safety can be ensured. Even if the gas leaks from the reformer 8 or the heating furnace 24, the gas is sent to the reformer 8 or the heating furnace 24 and burned together with the air from the air inlet 31.

FIG. 2 shows a system in which the hydrogen production apparatus (reformer) shown in FIG. 1 and a fuel cell are combined. In this hydrogen production apparatus, since the reforming catalyst layer 7, the CO shift catalyst layer 11, and the heating furnace 24 are integrated, the gas leaving the reforming apparatus is supplied to the second reformed gas cooler 13 at about 100 to 150 ° C. The CO is supplied to a CO selective oxidizer 15 filled with a CO selective oxidation catalyst 14, and CO is selectively oxidized by air to reduce it to about 10 ppm. Thereafter, the fuel passes through the hydrogen supply pipe 16 and is introduced into the fuel cell 18 as fuel. Since air is supplied to the fuel cell 18 from the air supply pipe 17, electricity is generated by a reaction between hydrogen and air. The gas containing unreacted hydrogen from the fuel cell 18 passes through the unreacted hydrogen discharge pipe 20 and is again supplied to the burner 23 of the heating furnace 24 and burned. Unreacted air is discharged from the fuel cell 18 to the atmosphere via an unreacted air pipe 19.

[0047]

According to the present invention, the thermal efficiency is improved, the heat insulating material is not required, or the thickness can be greatly reduced. In addition, since rapid startup can be achieved, it is possible to cope with a sudden load change, and it is possible to easily detect a gas leak, thereby ensuring high safety.

[Brief description of the drawings]

FIG. 1 is a structural diagram of a reformer according to an embodiment of the present invention.

FIG. 2 is a system diagram in which the reformer of the present invention and a fuel cell are combined.

FIG. 3 is a system diagram combining a conventional reformer and a fuel cell.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 Methane supply pipe 2 Water supply pipe 3 Steam supply pipe 4 Air supply pipe 5 Raw material supply pipe 6 Combustion catalyst layer 7 Reforming catalyst layer 8 Reformer 9 Reformed gas take-out pipe 10 First reformed gas cooler 11 CO conversion Catalyst layer 12 CO converter 13 Second reformed gas cooler 14 CO selective oxidation catalyst 15 CO selective oxidizer 16 Hydrogen supply pipe 17 Air supply pipe 18 Fuel cell 19 Unreacted air discharge pipe 20 Unreacted hydrogen discharge pipe 21 Heating furnace methane Supply pipe 22 Heating furnace air supply pipe 23 Burner 24 Heating furnace 25 Combustion furnace gas extraction pipe 30 Outer box 31 Air inlet 32 Air heating pipe 33 Heated air supply pipe 34 Methane heating pipe 35 Heated methane supply pipe 36 Water evaporation pipe 37 Saturation Steam supply pipe 38 Heated steam extraction pipe 39 Steam heating pipe 40 Blower 41 Partition wall

 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Yoshinori Otani 3-36 Takara-cho, Kure-shi, Hiroshima F-term in Babcock Hitachi, Ltd. Kure Research Laboratories 4G040 EA03 EA06 EA07 EB03 EB12 EB32 EB44 EB46 5H027 AA02 BA09 KK31

Claims (5)

[Claims] 1. A hydrogen production apparatus having a reformer for producing a hydrogen-rich gas by a reforming reaction with a hydrocarbon-based fuel, an oxygen-rich gas and water, wherein a hydrocarbon-based gas is provided on an outer peripheral portion of the reformer. A hydrogen production apparatus comprising a heating furnace for heating fuel, oxygen-rich gas and water. 2. A reformer and a heating furnace disposed on an outer periphery thereof are housed in an outer box, and the outer box, the reformer, and the heater are integrally formed, and a space is provided between the heating furnace and the outer box. 2. The hydrogen production apparatus according to claim 1, wherein a flow path is provided for introducing a gas present in the space into a combustion air supply section of the reformer and the heating furnace. 3. The heating furnace has a combustion section, an air heating pipe, and a fuel heating pipe arranged on an inner peripheral side partitioned by a partition having an open top, and a water evaporating pipe arranged on an outer peripheral side partitioned by a partition. 2. The hydrogen according to claim 1, wherein a combustion gas outlet is provided at a bottom portion of the heating furnace wall on the outer peripheral side, and a U-turn path for the combustion gas from the combustion portion is formed between the heating furnace ceiling surface and the partition wall. manufacturing device. 4. A gas detector is disposed in an outer box, and a thermometer is disposed in a heating furnace to detect a gas leak from the reformer or the heating furnace to activate an alarm device. The hydrogen production apparatus according to claim 1. 5. A flow path for introducing the reformed gas obtained by the hydrogen production apparatus according to claim 1 into a fuel cell via a CO selective oxidizer, and a gas containing unreacted hydrogen discharged from the fuel cell as hydrogen. A fuel cell system provided with a flow path for circulating supply to a heating furnace of a manufacturing apparatus.