JPH10297903A - Fuel reformer - Google Patents

Abstract

PROBLEM TO BE SOLVED: To rapidly improve the energy efficiency in a fuel reformer and rapidly heat up the fuel reformer into a stationary state at the time of starting a fuel cell. SOLUTION: The amount of methanol fed from a methanol tank 28 to an evaporating part 90 is limited at the time of starting a fuel reformer 22. Thereby, the heat quantity which is lost in the evaporating part 90 of a combustion gas fed from a burner 34 to the evaporating part 90 is suppressed and the resultant combustion gas is converted into a high-temperature combustion waste gas and discharged into a combustion waste gas introduction part 94. A reforming part 92 is rapidly heated up by utilizing the heat quantity of the high-temperature combustion waste gas. When the fuel reformer 22 is kept in a stationary state, the temperature of the combustion gas fed from the burner 34 is controlled to sufficiently reduce the temperature of the combustion waste gas discharged to the combustion waste gas introduction part 94.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fuel reforming apparatus, and more particularly, to a fuel reforming apparatus that reforms a raw fuel made of hydrocarbon into a hydrogen-rich fuel gas and supplies the fuel gas to a fuel cell.

[0002]

2. Description of the Related Art A fuel cell is a device that directly converts chemical energy of fuel into electrical energy without passing through mechanical energy or thermal energy, and can realize high energy efficiency. As a well-known form of a fuel cell, a pair of electrodes are arranged with an electrolyte layer interposed therebetween, and a fuel gas containing hydrogen is supplied to one electrode (the cathode side) and oxygen is supplied to the other electrode (the anode side). Is supplied, and an electromotive force is obtained by utilizing an electrochemical reaction occurring between both electrodes. The following shows an equation representing an electrochemical reaction occurring in a fuel cell. Equation (1) represents the reaction at the anode, and equation (2) represents the reaction at the cathode. The reaction represented by equation (3) proceeds in the entire fuel cell.

H ₂ → 2H ⁺ + 2e ⁻ (1) (1/2) O ₂ + 2H ⁺ + 2e ⁻ → H ₂ O (2) H ₂ + (1/2) O ₂ → H ₂ O (3) )

[0004] Fuel cells are classified according to the type of electrolyte used, operating temperature, and the like. Among these fuel cells, polymer electrolyte fuel cells, phosphoric acid fuel cells, molten carbonate electrolyte fuel cells, and the like. Alternatively, a reformed gas containing carbon dioxide can be used as a fuel gas. That is, a hydrogen-rich gas generated by reforming a hydrocarbon-based raw fuel such as methanol or natural gas can be used as a fuel gas. A fuel cell system including a fuel cell using a hydrocarbon-based raw fuel is provided with a fuel reformer, which reforms the raw fuel to generate a fuel gas. Hereinafter, the reforming reaction of the raw fuel in the fuel reformer will be described. Here, a case where methanol is used as a raw fuel and steam reforming is performed will be described.

CH ₃ OH → CO + 2H ₂ -90.0 (kJ / mol) (4) CO + H ₂ O → CO ₂ + H ₂ +40.5 (kJ / mol) (5) CH ₃ OH + H ₂ O → CO ₂ + 3H ₂ -49.5 (kJ / mol) (6)

[0006] In the reaction of steam reforming methanol,
The decomposition reaction of methanol represented by the formula (4) and the shift reaction of carbon monoxide represented by the formula (5) proceed simultaneously, and the reaction represented by the formula (6) occurs as a whole. As described above, since the reaction for reforming the raw fuel is an endothermic reaction, when performing the reforming reaction, it is necessary to supply the fuel required for the reaction to the fuel reformer.

As a method of supplying heat to the fuel reformer, a configuration is known in which a burner is provided in the fuel reformer and the reformer is heated by the combustion heat of the burner. JP-A-63-248702).
In such a fuel reformer, the temperature of the combustion gas of the burner is adjusted to raise the temperature of the reforming reactor for reforming the raw fuel to a desired temperature. Can be performed.

[0008]

However, in the above-described fuel reformer in which the reforming reaction of the raw fuel proceeds by using the combustion energy generated in the burner, the amount of heat energy supplied from the burner to the fuel reformer is reduced. Of these, a considerable amount is discharged without being used for the vaporization or reforming reaction of the raw fuel, resulting in a problem that the energy efficiency becomes insufficient. That is, since the reaction temperature at the time of performing the steam reforming of methanol is 250 to 300 ° C., the combustion temperature of the burner needs to be 300 ° C. or more. Exhaust gas was emitted and wasted without using much of the energy.

As a method of heating the fuel reforming apparatus, a heater may be provided instead of the burner, and the amount of heat required for the reforming reaction may be supplied by the heater. As described above, when heating is performed by providing a heater in the fuel reformer,
The amount of energy that is not used in the reforming reaction and discarded can be reduced, and the energy efficiency does not decrease. However, when the fuel reformer is heated using the heater as described above, it takes a long time to raise the temperature of the fuel reformer to a predetermined steady state when starting the fuel cell. There was a problem. In particular, when a fuel cell is used as a power source for driving an electric vehicle, the fact that it takes time to raise the temperature of the fuel reformer to a predetermined steady state means that the electric vehicle can be started. It takes time and it is hard to adopt.

The fuel reformer of the present invention solves such a problem, improves the energy efficiency of the fuel reformer, and raises the temperature of the fuel reformer to a steady state promptly at the start of the fuel cell. It was made for the purpose and adopted the following configuration.

[0011]

The fuel reforming apparatus of the present invention uses a hydrocarbon as a raw fuel, vaporizes at least a liquid containing the raw fuel, and generates a raw fuel gas. A fuel reforming apparatus that performs a reforming reaction that generates a fuel gas containing hydrogen from a fuel gas, and a calorie generation unit that generates a high-temperature gas capable of supplying a calorie required for vaporizing the liquid containing the raw fuel, The high-temperature gas generated by the heat generation unit and the liquid containing the raw fuel are supplied,
An evaporating unit configured to generate the raw fuel gas from the liquid by exchanging heat between the liquid and the high-temperature gas and to discharge exhaust gas generated after the high-temperature gas exchanges heat; A supply raw fuel amount control means for adjusting the amount of the liquid to be supplied to, and a predetermined reforming catalyst, receiving the supply of the raw fuel gas heated in the evaporator,
A reforming unit that advances the reforming reaction by passing the raw fuel gas through the surface of the reforming catalyst; a calorie moving unit that moves a calorie of the exhaust gas to the reforming unit; At the time of starting the apparatus, the amount of heat exchanged from the high-temperature gas to the liquid in the evaporator is reduced by limiting the amount of the liquid supplied to the evaporator through the raw fuel amount control means. The exhaust gas temperature raising control for setting the exhaust gas temperature to a predetermined high temperature is performed, and when the fuel reformer is in a steady state, the exhaust gas temperature raising control is performed for the amount of the liquid supplied to the evaporator. The gist of the present invention is to provide a non-control unit.

[0012] In the fuel reforming apparatus of the present invention configured as described above, the high-temperature gas generated by the calorific value generating section and the liquid containing at least the raw fuel are supplied to the evaporating section, and this liquid and the high-temperature high-temperature gas are supplied. Is exchanged with the other gases. Thereby, the liquid is vaporized and becomes a raw fuel gas. The high-temperature gas is discharged from the evaporator as exhaust gas after heat exchange. The raw fuel gas is supplied to a reforming section provided with a predetermined reforming catalyst, and the raw fuel gas passes through the surface of the reforming catalyst, whereby a reforming reaction proceeds, and a fuel gas containing hydrogen is generated. When the fuel reforming apparatus is started, exhaust gas temperature rise control is performed. That is, the amount of the liquid supplied to the evaporator is limited, and the amount of heat exchanged from the high-temperature gas to the liquid in the evaporator is reduced. As a result, the temperature of the exhaust gas discharged from the evaporator becomes a predetermined high temperature. The calorie of the exhaust gas which has reached a predetermined high temperature is moved to the reforming section by a calorie moving means. Also, when the fuel reformer enters a steady state,
The exhaust gas temperature raising control is not performed on the amount of the liquid supplied to the evaporator.

According to such a fuel reforming apparatus, when the fuel reforming apparatus is started, the amount of the liquid supplied to the evaporator is limited, so that the temperature of the exhaust gas becomes high. Accordingly, the temperature of the reforming unit to which the calorific value of the exhaust gas has been moved can be quickly raised to reach a steady state, and the time required for startup at startup can be reduced. Here, as means for raising the temperature of the exhaust gas,
Since the amount of the liquid to be supplied to the evaporator is limited, it is not necessary to prepare a burner having higher performance in order to raise the temperature of the exhaust gas at the time of starting the fuel reformer. Further, when the fuel reformer is in a steady state, the amount of the liquid supplied to the evaporator is not restricted with the aim of raising the exhaust gas temperature to a predetermined high temperature. Can be arbitrarily increased or decreased within a range corresponding to the amount of fuel gas that can be generated by the fuel reformer. Therefore, after the fuel reformer reaches the steady state, the generation of the required amount of fuel gas can be started.

Further, in the fuel reformer of the present invention,
When the fuel reformer is in a steady state and does not perform the exhaust gas temperature raising control on the amount of the liquid supplied to the evaporator, based on information on the amount of the liquid supplied to the evaporator, A high-temperature gas temperature control unit that controls the temperature of the high-temperature gas generated in the calorific value generating unit to reduce the temperature of the exhaust gas discharged from the evaporating unit to a predetermined temperature or less, and that the fuel reformer is in a steady state. It is also preferable to provide a heating means for supplying the amount of heat required for the reforming reaction to the reforming section when the above condition is satisfied.

According to such a fuel reforming apparatus, after a steady state is reached, the amount of heat required for the reforming reaction is supplied by the heating means. Therefore, compared with the case where the amount of heat required for the reforming reaction is also supplied by the high-temperature gas, the amount of energy that is not used and discarded outside the fuel reforming apparatus can be reduced, and the energy efficiency can be increased. it can. Thus, it is not necessary to supply heat to the reforming section by the exhaust gas discharged from the evaporating section,
The temperature of the high-temperature gas generated by the heat generation unit can be reduced, and the amount of energy consumed when generating the high-temperature gas can be reduced. Also,
Since the temperature of the exhaust gas discharged from the evaporator is equal to or lower than a predetermined temperature, the amount of energy discharged to the outside without being used in the fuel reformer can be reduced,
High energy efficiency can be maintained.

In the fuel reforming apparatus according to the present invention, the calorie transfer means is provided inside the reforming section, and selectively transfers heat from an exhaust gas discharged from the evaporating section toward the inside of the reforming section. It may be composed of a heat pipe formed so as to be transportable.

In such a fuel reformer, when the temperature of the exhaust gas discharged from the evaporator at the start of the fuel reformer is high, the amount of heat of the exhaust gas is transmitted to the inside of the reformer by the heat pipe. The temperature inside the reforming section can be quickly raised to a steady state. Also,
Since this heat pipe selectively performs heat transport in a direction from the exhaust gas side to the reforming section side, the temperature of the exhaust gas discharged from the evaporating section when the fuel reforming apparatus is in a steady state and the temperature inside the reforming section is increased. When the temperature is lower than the above range, no heat exchange is performed between the exhaust gas and the reforming section, and no heat is taken from the reforming section.

Further, in the fuel reforming apparatus according to the present invention, the heat transfer means is capable of introducing the exhaust gas, and heat exchange is performed between the introduced exhaust gas and the reforming section. An exhaust gas flow path, a second exhaust gas flow path capable of introducing the exhaust gas, and discharging the exhaust gas to the outside without exchanging heat with the reforming unit; At the time of starting, the flow path of the exhaust gas is the first exhaust gas flow path, and the amount of the liquid to be supplied to the evaporator is not controlled when the exhaust gas temperature control is performed.
A flow switching means for switching the flow path of the exhaust gas to the second exhaust gas flow path may be provided.

In such a fuel reformer, when the temperature of the exhaust gas discharged from the evaporator at the start of the fuel reformer is high, the exhaust gas is introduced into the first exhaust gas flow path, and the exhaust gas and the reformer are discharged. And heat exchange is carried out between them, and the temperature of the reforming section is quickly raised to a steady state. Further, when the fuel reformer enters a steady state, the exhaust gas discharged from the evaporator is introduced into the second exhaust gas channel, and the exhaust gas is discharged outside without heat exchange with the reformer. Therefore, when the temperature of the exhaust gas is lower than the temperature inside the reforming section, no heat is taken from the reforming section side to the exhaust gas side.

In the fuel reformer of the present invention, the heating means for supplying heat required for the reforming reaction when the fuel reformer is in a steady state is provided in the reformer. It may be a heater.

With this configuration, when the fuel reforming apparatus is started, the reforming section is quickly brought into a steady state by heating the reforming section using the high-temperature exhaust gas discharged from the evaporating section. In a steady state, the amount of heat required for the reforming reaction can be supplied using a heater provided in the reforming section. Therefore, in the steady state, the amount of energy that is not used in the fuel reformer and discarded can be reduced.

In the fuel reforming apparatus according to the present invention, the heating means for supplying heat required for the reforming reaction when the fuel reforming apparatus is in a steady state is provided inside the reforming section. It may be a means that utilizes the amount of heat generated by the progressing oxidative reforming reaction.

With this configuration, when the fuel reforming apparatus is started, the reforming section is quickly brought into a steady state by heating the reforming section using the high-temperature exhaust gas discharged from the evaporating section. In a steady state, the amount of heat required for the reforming reaction can be supplied by the oxidative reforming reaction. Therefore, in the steady state, the amount of energy that is not used in the fuel reformer and discarded can be reduced. In particular, since the oxidative reforming reaction that generates the amount of heat required for the reforming reaction proceeds inside the reforming section, the amount lost during the transfer of energy can be reduced, and high energy efficiency can be obtained. it can.

In the fuel reformer of the present invention, the raw fuel may be methanol. Since methanol can perform a reforming reaction at a relatively low temperature among hydrocarbon-based raw fuels, it is preferable when methanol is used for applications that require repeated operation and shutdown of the fuel reformer. Also, comparing the amount of energy obtained from a predetermined volume of the hydrocarbon-based raw fuel, methanol is a raw fuel having a large amount of energy obtained from the reformed gas generated in the reforming reaction. Therefore, when the fuel reforming device is mounted on a vehicle and the fuel reforming device is used for an application involving movement, such as when the fuel reforming device supplies a fuel gas to a fuel cell which is a power source for driving the vehicle, Is advantageous.

Further, in the fuel reforming apparatus of the present invention, the liquid containing the raw fuel is a mixture of the raw fuel and water in a liquid state or a mixed substance of the raw fuel and water in a gas state. The reforming reaction that proceeds in the reforming section may include at least a steam reforming reaction.

Here, the liquid containing at least the raw fuel supplied to the evaporator only needs to contain at least the liquid component and the raw fuel component, and may contain other gas components and the like. . When the reforming reaction includes at least the steam reforming reaction, water required for the steam reforming reaction is contained at least as a liquid component. For example, when a raw fuel composed of a liquid hydrocarbon such as methanol is used, the liquid is a mixture of water and a liquid raw fuel required for the steam reforming reaction. When a raw fuel composed of a gaseous hydrocarbon such as methane is used, the liquid is a mixture of water and a gaseous raw fuel required for the steam reforming reaction. Further, a gas containing oxygen required for the partial oxidation reforming reaction may be added thereto. It is not necessary to mix all of the components constituting the liquid containing the raw fuel and supply them to the evaporator in advance. The temperature or only the temperature rise may be performed.

[0027]

DESCRIPTION OF THE PREFERRED EMBODIMENTS In order to further clarify the structure and operation of the present invention described above, embodiments of the present invention will be described below based on examples. FIG. 1 is a schematic configuration diagram illustrating a schematic configuration of a fuel cell system 20 according to a preferred embodiment of the present invention. Fuel cell system 20 of the present invention
The fuel reformer has a configuration in which the internal temperature is rapidly increased by the combustion gas generated by the burner when the system is started, and the amount of energy generated by the burner is reduced in a steady state to reduce the amount of energy to be discarded outside. It is characterized by having. First, the overall configuration of the fuel cell system 20 will be described, and subsequently, a fuel reformer corresponding to a main part of the present invention will be described.

The fuel cell system 20 includes a methanol tank 28 for storing methanol and a water tank 3 for storing water.
0, a burner 34 for generating combustion gas, a compressor 32 for compressing air, a fuel reformer 22 equipped with a burner 34 and a compressor 32 for performing a methanol reforming reaction, and a monoxide in the reformed gas. A CO reduction unit 26 for reducing carbon concentration, a fuel cell 40 for obtaining an electromotive force by an electrochemical reaction, an air tank 36 for storing compressed air, a compressor 38 for supplementarily supplying compressed air, and a control unit 50 including a computer are mainly included. Components. Hereinafter, the components of the fuel cell system 20 will be sequentially described.

The fuel cell 40 is a solid polymer electrolyte type fuel cell, and has a stack structure in which a plurality of unit cells 48 as constituent units are stacked. FIG. 2 is a cross-sectional view illustrating the configuration of a single cell 48 of the fuel cell 40. The single cell 48 includes an electrolyte membrane 41, an anode 42 and a cathode 43, and separators 44 and 45.

The anode 42 and the cathode 43 are gas diffusion electrodes having a sandwich structure sandwiching the electrolyte membrane 41 from both sides. The separators 44 and 45 form a flow path for the fuel gas and the oxidizing gas between the anode 42 and the cathode 43 while further sandwiching the sandwich structure from both sides. A fuel gas flow path 44P is formed between the anode 42 and the separator 44,
An oxidizing gas flow path 45P is formed between 3 and the separator 45. Although the separators 44 and 45 each have a flow path formed on only one side in FIG. 2, ribs are actually formed on both sides thereof, and a fuel gas flow path 44 P is formed on one side with the anode 42. The other surface forms an oxidizing gas flow channel 45P with the cathode 43 provided in the adjacent single cell. As described above, the separators 44 and 45 have a function of forming a gas flow path between the gas diffusion electrodes and separating the flows of the fuel gas and the oxidizing gas between the adjacent single cells. Of course, when stacking the unit cells 48 to form a stack structure, the two cells located at both ends of the stack structure
The ribs may be formed only on one side of the separator in contact with the gas diffusion electrode.

Here, the electrolyte membrane 41 is a proton-conductive ion exchange membrane formed of a solid polymer material, for example, a fluorine-based resin, and has good electric conductivity in a wet state. In this embodiment, a Nafion membrane (manufactured by DuPont) is used.
It was used. The surface of the electrolyte membrane 41 is coated with platinum as a catalyst or an alloy made of platinum and another metal. As a method of applying the catalyst, a carbon powder supporting platinum or an alloy composed of platinum and another metal is prepared, and the carbon powder supporting the catalyst is dispersed in an appropriate organic solvent, and an electrolytic solution (eg, Aldrich Chemi) is used.
Cal Co., Nafion Solution) was added in an appropriate amount to form a paste, and screen printing was performed on the electrolyte membrane 41. Alternatively, a configuration in which a paste containing the carbon powder supporting the catalyst is formed into a film to form a sheet and the sheet is pressed on the electrolyte membrane 41 is also suitable.

The anode 42 and the cathode 43 are both formed of carbon cloth woven with carbon fiber yarns. In the present embodiment, the anode 42 and the cathode 43 are formed of carbon cloth, but a configuration formed of carbon paper or carbon felt made of carbon fiber is also suitable.

The separators 44 and 45 are made of a gas-impermeable conductive member, for example, dense carbon which is made by compressing carbon to be gas-impermeable. Separator 4
4, 45 have a plurality of ribs arranged in parallel on both surfaces thereof. As described above, the fuel gas flow path 44P is formed with the surface of the anode 42, and the cathode 43 of the adjacent single cell is formed. And an oxidizing gas flow path 45P. Here, the ribs formed on the surface of each separator need not be formed in parallel on both surfaces, and may be at a predetermined angle such as perpendicular to each surface. The ribs do not have to be parallel grooves, but may be any as long as a fuel gas or an oxidizing gas can be supplied to the gas diffusion electrode.

The configuration of the single cell 48 which is the basic structure of the fuel cell 40 has been described above. When the fuel cell 40 is actually assembled, the separator 44, the anode 4
2. A plurality of single cells 48 composed of an electrolyte membrane 41, a cathode 43, and a separator 45 are stacked in this order (100 pairs in this embodiment), and a current collector plate formed of a dense carbon or copper plate at both ends thereof By arranging 46 and 47, a stack structure is formed.

Next, components other than the fuel cell 40 constituting the fuel cell system 20 and their connection relationships will be sequentially described. The fuel reformer 22 includes an evaporator 90 and a reformer 92, as shown in FIG. The evaporating section 90 receives supply of methanol and water from the methanol tank 28 and the water tank 30, and vaporizes the methanol and water. Further, in the reforming section 92, the methanol and water vaporized in the evaporating section 90 are guided, and a steam reforming reaction proceeds. The fuel reformer 22 includes the burner 34 and the compressor 32 as described above.
As will be described later, the heat of combustion of the burner 34 is guided to the evaporator 90 via the compressor 32, and the heat of combustion is transmitted to the heat exchange unit of the evaporator 90, and the methanol and water supplied to the evaporator 90 And boil and evaporate.

From the methanol tank 28 to the fuel reformer 2
A second pump 65 is provided in a methanol flow path 70 that feeds the raw fuel methanol to the fuel cell 2, and the amount of methanol supplied to the fuel reformer 22 can be adjusted. The second pump 65 is connected to the control unit 50, and is driven by a signal output from the control unit 50,
The flow rate of methanol supplied to the fuel reformer 22 is adjusted.

A third pump 66 is provided in a water supply channel 72 for feeding water from the water tank 30 to the fuel reformer 22, and the amount of water supplied to the fuel reformer 22 can be adjusted. The third pump 66 is connected to the control unit 50 similarly to the second pump 65, is driven by a signal output from the control unit 50, and adjusts the amount of water supplied to the fuel reformer 22. The methanol flow path 70 and the water supply path 72 join to form a first fuel supply path 78, which is connected to the evaporator 90 of the fuel reformer 22. The flow rate of methanol and the flow rate of water depend on the second pump 65.
And the third pump 66, the methanol and water mixed by a predetermined amount are supplied to the fuel reformer 22 via the first fuel supply path 78. In addition, the mixing ratio of methanol and water depends on the above-described formula (4).
The amount of the steam reforming reaction shown in the equation (6) is sufficient to allow the steam reforming reaction to proceed sufficiently.
Is determined as an amount that allows a sufficient amount of water vapor to be contained as fuel gas supplied to the fuel cell.

The compressor 32 attached to the fuel reformer 22
Is a device for taking in air from outside the fuel cell system 20, compressing it, and supplying it under pressure to the air tank 36. The compressor 32 includes a turbine 32a and a compressor 32b, which are formed in an impeller shape. The turbine 32a and the compressor 32b are connected by a coaxial shaft 32c, and the compressor 32b can be rotationally driven by rotationally driving the turbine 32a. The fuel reformer 22 is further provided with a burner 34, and the high temperature combustion gas from the burner 34 drives the turbine 32a.

The compressor 32b also rotates with the rotation of the turbine 32a, and the compressor 32b compresses air as described above. Outside air can be taken into the compressor 32b via the air introduction path 69.

Here, since the turbine 32a is driven by the high-temperature combustion gas from the burner 34, it is made of a super heat-resistant alloy, ceramics or the like in order to realize heat resistance and durability. In this embodiment, a nickel-based alloy (Inconel 700, Inc.) was used. The compressor 32b is made of a lightweight aluminum alloy.

The compressed air pressurized by the compressor 32 is once supplied to the air tank 36 and then supplied to the burner 34 and the oxygen electrode side of the fuel cell 40 as described later. The air tank 36 is provided with a pressure sensor 67 for measuring the air pressure in the air tank 36, and further provided with a compressor 38 for compensating for an insufficient amount of air in the air tank 36. The pressure sensor 67 is connected to the control unit 50. Control unit 50
Determines the amount of air in the air tank 36 based on the input signal from the pressure sensor 67, and outputs a drive signal to the compressor 38 when it is determined that the amount of air is insufficient. Control is performed so that the amount of supplied compressed air is sufficient. When the fuel cell system 20 is operating in a steady state, the air tank 36
Since a sufficient amount of compressed air can be supplied from the compressor 2, the compressor 38 is mainly used when the system is started.

The burner 34 for driving the turbine 32a is
Fuel for combustion is supplied from the cathode side of the fuel cell 40 and the methanol tank 28. The fuel cell 40 performs an electrochemical reaction using hydrogen-rich gas generated by reforming methanol in the fuel reformer 22 as fuel. However, not all hydrogen supplied to the fuel cell 40 is consumed. The fuel exhaust gas containing the remaining hydrogen is discharged from the fuel exhaust gas passage 74. The burner 34 is connected to the fuel exhaust gas passage 74 to receive the supply of the fuel exhaust gas, and to completely burn the remaining hydrogen that has not been consumed, thereby improving the fuel utilization rate. The burner 34 supplies the methanol from the methanol tank 28 when the exhausted fuel alone is insufficient for the fuel, and when the supply of the exhausted fuel from the fuel cell 40 cannot be received such as when the fuel cell system 20 is started. receive. A methanol branch 71 is provided for supplying methanol to the burner 34. The methanol branch 71 is a methanol passage 70 for supplying methanol from the methanol tank 28 to the fuel reformer 22.
And a first pump 64 is provided. First
The pump 64 is connected to the control unit 50, and adjusts the amount of methanol supplied to the burner 34 in response to a drive signal from the control unit 50.

On the other hand, the burner 34 receives supply of oxygen necessary for combustion in addition to the fuel for combustion. Oxygen necessary for this combustion is supplied as compressed air from the above-described air tank 36 via the first air supply path 76. A first flow regulator 68 is provided in the first air supply passage 76, and the first flow regulator 68 adjusts the amount of compressed air supplied to the burner 34 by receiving a drive signal from the control unit 50. doing.

Here, the first temperature sensor 6 is connected to the burner 34.
0 is provided, the temperature of the combustion gas in the burner 34 is measured, and the measurement result is converted into an electric signal by the control unit 5.
0 is input. The control unit 50 controls the first pump 64 and the first pump 64 based on the input result from the first temperature sensor 60.
A drive signal is output to the flow controller 68 to adjust the amount of methanol and the amount of compressed air supplied to the burner 34, and
The combustion temperature at 4 is maintained in a predetermined temperature range described later. The combustion gas in the burner 34 is supplied to the turbine 32
a, and then the evaporating section 90 of the fuel reformer 22 is rotated.
It is led to. Since the heat exchange efficiency in the turbine 32 a is not so high (within about 10%), much of the heat energy generated in the burner 34 is guided to the evaporator 90. In the evaporator 90, the mixed solution of methanol and water supplied through the first fuel supply passage 78 is vaporized by the high-temperature combustion exhaust gas supplied from the burner 34. Evaporator 90
The raw fuel gas consisting of methanol and water vaporized in
The fuel is supplied to the reforming section 92 in the fuel reformer 22.

In the reforming section 92 provided in the fuel reformer 22, a raw fuel gas comprising methanol and water is supplied, and the steam reforming reaction shown in the equations (4) to (6) proceeds to A rich reformed gas is generated. This reformer 92
Will be described later in detail. The reformer 92 is provided with an electric heater as a means for heating the inside in addition to being supplied with the combustion gas generated by the burner 34 as described above, and the fuel reformer 22 is brought into a steady state. When
This heater makes it possible to maintain the inside of the reforming section 92 at a temperature suitable for the steam reforming reaction.

The hydrogen-rich reformed gas reformed in the reforming section 92 is guided to the CO reducing section 26 through the second fuel supply path 79. The second temperature sensor 61 provided in the second fuel supply path 79 measures the temperature of the reformed gas discharged from the reforming section 92, and inputs information on the measurement result to the control section 50. The control unit 50 determines the reaction temperature inside the reforming unit 92 based on the signal from the second temperature sensor 61, and controls the above-described predetermined heating means included in the reforming unit 92 to control the reforming unit 92.
Is maintained within a predetermined temperature range.

The CO reducing unit 26 reduces the carbon monoxide concentration of the reformed gas supplied from the reforming unit 92 via the second fuel supply passage 79 to obtain a fuel gas having a sufficiently low carbon monoxide concentration. This is a device for supplying to the fuel cell 40. The general reforming reaction of methanol has already been shown in equations (4) to (6). However, when the reforming reaction is actually performed, the reaction does not proceed ideally as shown in these equations. Instead, the fuel gas generated in the reforming section 92 contains a predetermined amount of carbon monoxide. Therefore, by providing the CO reduction unit 26, the concentration of carbon monoxide in the fuel gas supplied to the fuel cell 40 is reduced.

The fuel cell 40 of this embodiment is a polymer electrolyte fuel cell, which is provided with a catalyst composed of platinum or platinum and another metal which promotes the cell reaction. Was applied to the surface of the electrolyte membrane 41), and when carbon monoxide was contained in the fuel gas, this carbon monoxide was adsorbed on the platinum catalyst to reduce the function as a catalyst,
The reaction at the anode shown in the equation (1) is hindered and the performance of the fuel cell is reduced. Therefore, the fuel cell 4
In order to perform power generation using a polymer electrolyte fuel cell such as 0, it is essential to reduce the carbon monoxide concentration in the supplied fuel gas to a predetermined amount or less to prevent a decrease in cell performance. . In such a polymer electrolyte fuel cell, the allowable concentration as the concentration of carbon monoxide in the supplied fuel gas is usually about several ppm or less.

The reformed gas supplied to the CO reduction unit 26 is
As described above, the gas is a hydrogen-rich gas containing a predetermined amount of carbon monoxide, and the CO reduction unit 26 oxidizes carbon monoxide in preference to hydrogen in the reformed gas. CO
The reduction unit 26 is filled with a carrier that supports a platinum catalyst, a ruthenium catalyst, a palladium catalyst, a gold catalyst, or an alloy catalyst using these as the first element, which are selective oxidation catalysts for carbon monoxide. The oxidizing gas containing oxygen required for the selective oxidation reaction of carbon monoxide in the CO reduction unit 26 is supplied from the air tank 36 as compressed air. A third flow rate regulator 84 is provided in a third air supply path 82 which is a flow path connecting the air tank 36 and the CO reduction unit 26, so that the amount of compressed air supplied to the CO reduction unit 26 can be adjusted. ing. The third flow regulator 84 is connected to the control unit 50, and the driving amount of the third flow regulator 84 is controlled by the control unit 5.
Controlled by 0.

Since the selective oxidation reaction of carbon monoxide performed in the CO reduction unit 26 is an exothermic reaction, the CO reduction unit 26 is provided with a predetermined cooling means, and the inside of the CO reduction unit 26 is selectively oxidized. The temperature is kept within a predetermined temperature range suitable for the temperature. As the predetermined cooling means, for example, it is possible to use a configuration in which water stored in the water tank 30 is used as cooling water, and the cooling water is circulated through a flow path provided in the CO reduction unit 26.

The carbon monoxide concentration in the fuel gas processed by the CO reduction unit 26 is determined by the operating temperature of the CO reduction unit 26, the carbon monoxide concentration in the supplied reformed gas, and the CO reduction unit 26.
Determined by the supply flow rate of the reformed gas per unit catalyst volume to the catalyst. The CO reduction unit 26 is provided with a fourth temperature sensor 63 and a carbon monoxide concentration sensor (not shown). Based on the measurement result of the carbon monoxide concentration sensor,
The operating temperature of the reducing section 26 and the flow rate of the reformed gas to be supplied are adjusted to control the concentration of carbon monoxide in the processed fuel gas to be equal to or less than an allowable value.

The fuel gas whose carbon monoxide concentration has been reduced as described above in the CO reduction unit 26 is guided to the fuel cell 40 by the third fuel supply path 80 and is subjected to a cell reaction on the anode side. A third temperature sensor 62 is provided in the third fuel supply path 80, and the temperature of the fuel gas discharged from the CO reduction unit 26 is measured by the third temperature sensor 62. Information about the temperature of the fuel gas detected by the third temperature sensor 62 is input to the control unit 50, and is provided to a process for controlling the operating temperature of the CO reduction unit 26.

Further, a fuel branch passage 81 branches from the third fuel supply passage 80, and a three-way switching valve 37 is provided at a branch point of the fuel branch passage 81. Fuel branch 8
1 is connected to the burner 34, and switches the three-way switching valve 37 to switch the flow path of the fuel gas discharged from the CO reduction unit 26 and supply the fuel gas to the fuel cell 40. Fuel gas is burner 3
4 can be set to any of the states supplied to the power supply 4. The three-way switching valve 37 is connected to the control unit 50, and the control unit 50 switches the fuel gas flow path by outputting a drive signal to the three-way switching valve 37. The state in which the fuel gas is supplied to the fuel cell 40 is as follows.
The state in which the fuel cell system 20 is in a steady state corresponds to the state in which the fuel gas is supplied to the burner 34 when the fuel cell system 20 is started. Will be explained in detail later

On the other hand, the oxidizing gas related to the cell reaction on the cathode side of the fuel cell 40 is supplied from the air tank 36 to the second
It is supplied as compressed air via an air supply path 77. A second flow regulator 83 is provided in the second air supply path 77 so that the amount of oxidizing gas supplied from the air tank 36 to the fuel cell 40 can be adjusted. The second flow regulator 83 is connected to the control unit 50, and the control unit 50 controls the amount of the oxidizing gas supplied to the fuel cell 40. The oxidizing gas becomes an oxidizing exhaust gas after being subjected to the battery reaction and is discharged to the oxidizing exhaust gas passage 73. The oxidizing exhaust gas passage 73 is provided with a condensed water collector 24. When the electrochemical reaction proceeds in the fuel cell 40, water is generated on the oxygen electrode side of the fuel cell 40 by the reaction of the above-described equation (2).
In the fuel cell system 20 of the present embodiment, the oxidized exhaust gas containing the water generated by the cell reaction is led to the condensed water collector 24 to condense and recover the water generated in the oxidized exhaust gas, and the collected water is reused. ing. The produced water recovered by the condensed water recovery unit 24 is supplied to the water tank 30 via the water recovery path 35, and is supplied to the steam reforming reaction of the raw fuel performed in the reforming unit 92 via the evaporating unit 90. . The oxidized exhaust gas from which the generated water has been recovered by the condensed water recovery device 24 is supplied to a burner 34 via an exhaust gas recovery path 33. Since oxygen remains in the oxidizing exhaust gas discharged after being subjected to the electrochemical reaction in the fuel cell 40, the oxidizing exhaust gas supplied to the burner 34 functions as an oxidizing gas required for a combustion reaction in the burner 34. .

The control unit 50 is configured as a logic circuit centered on a microcomputer. More specifically, the control unit 50 executes a predetermined operation according to a preset control program, and the CPU 54 executes various operations. A ROM 56 in which necessary control programs, control data, and the like are stored in advance, and an R for temporarily reading and writing various data necessary for performing various arithmetic processing by the CPU 54.
The AM 58 and the input / output port 52 for inputting detection signals from the various temperature sensors and pressure sensors described above and outputting drive signals to the various pumps and flow rate regulators described above in accordance with the calculation results of the CPU 54 are provided. Prepare.

Although not shown in FIG. 1, the fuel cell system 20 includes a predetermined secondary battery separately from the fuel cell 40. This secondary battery is a fuel cell system 20
When sufficient power cannot be supplied from the fuel cell 40 at the time of startup, the power is used as a power source for driving the compressor 38 and various pumps described above.

Next, the configuration of the fuel reformer 22 corresponding to the main part of the present invention will be described. FIG. 3 is an explanatory diagram schematically showing the configuration of the fuel reforming device 22. The fuel reformer 22 includes the evaporator 90 and the reformer 92 as described above.
Is provided. The combustion gas supplied from the burner 34 via the compressor 32 is guided to the evaporating section 90, where the temperature of the mixed liquid of methanol and water supplied via the first fuel supply path 78 is raised and vaporized. Raw fuel gas. The evaporating section 90 is formed in a plate-fin shape, and the flow direction of the combustion gas supplied from the burner 34 and the flow path of the mixed liquid of methanol and water are set so that the respective flow directions are substantially opposite. It is arranged to become. Therefore, heat exchange is performed between the combustion gas flowing in different directions from each other and the mixed liquid,
The mixed liquid of methanol and water becomes a raw fuel gas whose temperature has been sufficiently raised. As described above, since the flow directions of the combustion gas and the mixed liquid are opposite to each other, the evaporator 90
The liquid mixture introduced to the above starts heat exchange with the downstream combustion gas that is relatively low in temperature, and is gradually vaporized while exchanging heat with the higher temperature combustion gas as it proceeds to the upstream side. . Finally, the raw fuel gas is heated by a sufficiently high temperature gas on the upstream side of the combustion gas guided to the evaporating section 90, and is introduced into the reforming section 92.

The combustion gas whose temperature has been reduced by the heat exchange in the evaporating section 90 is discharged from the evaporating section 90 to the flue gas introducing section 94 as combustion exhaust gas. The combustion exhaust gas introduction unit 94 has a structure provided in a lower region of an outer peripheral portion of the fuel reformer 22. The flue gas is guided in the flue gas introducing section 94 in the same direction as the raw fuel gas passes through the reforming section 92, and reaches the end of the fuel reforming apparatus 22. Is discharged. Further, the flue gas introducing section 94 has a structure that enables heat exchange between the flue gas passing through the flue gas introducing section 94 and the inside of the reforming section 92. This flue gas introduction part 94
A structure that enables heat exchange between the combustion exhaust gas passing through the inside and the inside of the reforming section 92 will be described later.

The reforming section 92 is filled with pellets formed of a Cu—Zn catalyst, which is a catalytic metal for accelerating the reforming reaction. Reaction to generate a hydrogen-rich reformed gas. Here, a pellet formed of a catalyst metal, a Cu-Zn catalyst, refers to a catalyst metal prepared by a coprecipitation method using copper and zinc oxide, adding a binder such as alumina, and extruding to a diameter of 3 to 3 mm. It is formed into a particle of about 7 mm. In this embodiment, about 3 mm × 3 m
A pellet molded to a size of mx 3 mm was used. The pellet made of the Cu—Zn catalyst is uniformly filled in the reforming section 92. The raw fuel gas introduced into the reforming section 92 moves toward the outlet direction leading to the second fuel supply passage 79 while making contact with the catalyst metal on the pellet surface and progressing the reforming reaction. The catalyst pellets to be filled in the reforming section 92 may be prepared by other methods such as the impregnation method in addition to the coprecipitation method described above.

Here, a structure that enables heat exchange between the combustion exhaust gas passing through the combustion exhaust gas introduction unit 94 and the inside of the reforming unit 92 will be described. A heat pipe 96 is further provided inside the reforming section 92 filled with the catalyst pellets. The heat pipe 96 is disposed in a direction perpendicular to the flow of the raw fuel gas in which the reforming reaction is progressing, with one end of the heat pipe 96 projecting into the flue gas introducing section 94. Inside, a plurality of heat pipes 96 are provided at predetermined intervals. In each heat pipe 96, a fin 98 is provided at an end protruding from the flue gas introduction portion 94. In this embodiment, the fins 98 are made of stainless steel.
The fins 98 are formed as wing-shaped members protruding from the surface of each heat pipe 96 in a direction perpendicular to the heat pipes, and a plurality of (four in FIG. 3) fins 98 are provided for each heat pipe 96. Have been. When the combustion exhaust gas discharged from the evaporating section 90 passes through the combustion exhaust gas introduction section 94, the calorie of the combustion exhaust gas projects through the fins 98 to the end of the heat pipe 96 (projects into the combustion exhaust gas introduction section 94. End).

The heat pipe 96 provided with the fins 98 includes water, naphthalene, or diphenyl heat medium oil as a working fluid, and is configured as a wickless heat pipe. In a heat pipe of this type, when heat is transmitted to the lower end, the working fluid is vaporized and rises in the heat pipe. The rising working fluid loses heat above the heat pipe and liquefies, and returns downward by gravity. As described above, since the reflux of the working fluid occurs only by gravity, heat transport is selectively performed from below to above. Therefore, when the temperature of the flue gas passing through the flue gas introduction section 94 is higher than the internal temperature of the reforming section 92, heat exchange is performed between the flue gas and the inside of the reforming section 92. Meanwhile, when the temperature of the flue gas passing through the flue gas introduction portion 94 is lower than the internal temperature of the reforming portion 92, no heat exchange is performed between the two.

As described above, since the fins 98 have a structure for transmitting the heat of the combustion exhaust gas to the end of the heat pipe 96, the heat of the combustion exhaust gas is transmitted to the end of the heat pipe 96 with sufficient efficiency. If possible, it may be formed in a shape different from the above description. Also,
The fins 98 can transmit the heat of the flue gas to the end of the heat pipe 96 with sufficient efficiency and have sufficient heat resistance to the temperature of the flue gas passing through the flue gas introduction portion 94. You may comprise with members other than the said stainless steel.

Next, the operation of the fuel cell system 20 according to the present embodiment when the system is started will be described. FIG.
5 is a flowchart illustrating a start-time processing routine executed when the fuel cell system 20 is started. This routine is executed when the start of the system is instructed from a predetermined start switch in the fuel cell system 20.
4 is performed. When this routine is started, first, a drive signal is output to the compressor 38, and the compressor 38 is started (step S100). When the compressor 38 is activated, the air tank 36 is activated.
, The supply of pressurized air is started. At this time, a drive signal is output to the three-way switching valve 37, and the flow path of the fuel gas discharged from the CO reduction unit 26 is
The flow is switched to the flow path in which the fuel gas is supplied to the burner 34 (Step S110).

Next, the pressure P1 in the air tank 36 measured by the pressure sensor 67 of the air tank 36 is read (step S120), and the read value P1 and the control unit 5
It is compared with a predetermined reference value P0 stored in 0 (step S130). The predetermined reference value P0 is predetermined as a pressure in the air tank 36 when a sufficient amount of air is stored in the air tank 36 to supply compressed air to each part of the fuel cell system 20. Value. When the pressure P1 is lower than the predetermined reference value P0, the process returns to step S120, and the above processing is repeated until the pressure in the air tank 36 is sufficiently increased.

In step S130, the air tank 36
When the pressure P1 in the inside becomes equal to or more than the reference value P0,
It is determined that a sufficient amount of compressed air has been stored in the air tank 36, and then a combustion reaction is started in the burner 34 (step S140). When starting the combustion reaction in the burner 34, a drive signal is output to the first pump 64 to start supplying methanol to the burner 34, and a drive signal is output to the first flow regulator 68 to output the burner 3.
The supply of compressed air to the burner 4 is started, and ignition is performed by a predetermined ignition device provided in the burner 34. Thereafter, the drive amounts of the first pump 64 and the first flow regulator 68 are such that the amounts of methanol and water supplied to the burner 34 are such that the burner 34 generates a sufficiently large predetermined combustion energy. Is controlled. Thereafter, the driving state of the compressor 38 is controlled based on the value of the pressure P1 in the air tank 36 read by the pressure sensor 67 so that the amount of compressed air stored in the air tank 36 is maintained within a predetermined range. You.

When the combustion reaction in the burner 34 is started,
The combustion temperature t1 at the burner 34 detected by the first temperature sensor 60 is read (step S150). Next, the combustion temperature t1 of the burner 34 is compared with a predetermined reference value t0 stored in the control unit 50 (step S5).
160). The predetermined reference value t0 is a value determined in advance as a temperature at which the combustion state in the burner 34 becomes sufficient. Here, the sufficient combustion state is a temperature at which the reforming section 92 can be rapidly heated by the combustion exhaust gas discharged from the evaporating section 90 as described later. In this embodiment, the temperature is within a temperature range of about 600 to 800 ° C. Was set.
When the combustion temperature t1 is lower than the predetermined reference value t0, the process returns to step S150, and while adjusting the amount of methanol and the amount of compressed air supplied to the burner 34 until the combustion temperature of the burner 34 sufficiently rises, the above-mentioned combustion temperature is adjusted. The processing of reading t1 and comparing it with the reference value t0 is repeated.

In step S160, the combustion temperature t1
Is equal to or greater than the reference value t0, it is determined that the combustion temperature in the burner 34 has risen sufficiently. Next, a drive signal is output to the second pump 65 and the third pump 66 to execute this routine. End (step S17)
0). By driving the second pump 65 and the third pump 66, the supply of methanol and water to the evaporator 90 is started. At this time, the amount of methanol and water supplied to the evaporating section 90 is one third to one third of the amount that can be sufficiently vaporized and heated by the combustion gas supplied from the burner 34 via the compressor 32. 2 can be suppressed.
Therefore, the flue gas discharged from the evaporating section 90 to the flue gas introduction section 94 after performing heat exchange between methanol and water to evaporate and raise the temperature thereof still has a large amount of heat energy. I have. Fuel reformer 2 of the present embodiment
In (2), the temperature of the flue gas discharged to the flue gas introduction section 94 is about 300 to 500 ° C.

The flue gas discharged to the flue gas introduction part 94 exchanges heat with the fin 98 provided at the end of the heat pipe 96 in the flue gas introduction part 94. The amount of heat transferred to the fins 98 in this way is transferred to the inside of the reforming section 92 via the heat pipe 96, and the inside of the reforming section 92 is heated. As described above, the flue gas introduced into the flue gas introduction unit 94 when the fuel cell system 20 is activated is approximately 300 to 500 ° C.
, The temperature inside the reforming section 92 quickly rises.

In step S170, when the supply of methanol and water to the evaporator 90 is started, the raw fuel gas composed of methanol and water evaporated in the evaporator 90 is supplied to the reformer 92. It is subjected to a steam reforming reaction. At this time, since the heating of the reforming section 92 by the high-temperature combustion exhaust gas described above is rapidly performed, the raw fuel gas expressed by the equations (4) to (6) Gradually proceeds. As described above, while the temperature of the reforming section 92 is not sufficiently raised, the reforming reaction progressing in the reforming section 92 becomes insufficient.
The concentration of hydrogen in the reformed gas supplied to the CO reduction unit 26 via the fuel supply path 79 is insufficient as the fuel gas supplied to the fuel cell 40. In step S110, since the three-way switching valve 37 has been switched to the above-described state, when the fuel cell system 20 is started, the fuel gas having an insufficient hydrogen concentration is supplied to the fuel cell 40 instead of being supplied to the fuel cell 40. Is supplied to the burner 34 and is used as fuel for a combustion reaction.

Next, the operation when the operating state of the fuel cell system 20 becomes a steady state will be described. FIG.
4 is a flowchart illustrating a temperature-raising processing routine executed after the fuel cell system is started. This routine is executed after the start-up processing routine described above is completed.
Performed by U54. When this routine is started, first, the CPU 54 inputs the reformed gas temperature t2 detected by the second temperature sensor 61 (step S20).
0). The temperature of the reformed gas detected by the second temperature sensor 61 reflects the internal temperature of the reforming section 92 well, and the heating state of the reforming section 92 can be known from the temperature t2 of the reformed gas. . Therefore, next, the state of the internal temperature of the reforming section 92 is determined by comparing the reformed gas temperature t2 with a predetermined reference value t3 (step S210).

The predetermined reference value t 3 is a reformed gas temperature when the inside of the reforming section 92 is heated to a temperature at which the steam reforming reaction can proceed with sufficient efficiency on the catalyst surface. This is a predetermined value. In this embodiment, the reference value t3 is set to about 250 ° C. If the temperature t2 of the reformed gas is lower than the predetermined reference value t3, step S
Returning to 200, until the temperature of the reformed gas rises sufficiently
Reading of the reformed gas temperature t2 and the reference value t
Repeat the process of comparison with 3. At this time, the reforming unit 9
As described above, since the thermal energy is transmitted from the high-temperature combustion exhaust gas through the fins 98 and the heat pipes 96, the internal temperature of the reforming section 92, that is, the second temperature sensor 61 detects the thermal energy. The quality gas temperature is rising rapidly.

In step S210, when the temperature t2 of the reformed gas becomes equal to or higher than the reference value t3, it is determined that the internal temperature of the reforming section 92 has risen to a degree sufficient for the reforming reaction to proceed. Next, the control regarding the amounts of methanol and water supplied to the evaporating unit 90 is changed (step S220). That is, the restriction on the drive amount of the second pump 65 and the third pump 66 is stopped. As described above, when the fuel cell system 20 is started, the amount of heat generated by the burner 34 is maintained at a predetermined value, and the amounts of methanol and water supplied to the evaporator 90 are controlled by the burner 34 via the compressor 32. Is reduced to one third to two thirds of the amount that can be sufficiently vaporized and heated by the combustion gas supplied from the fuel cell. Executing step S220 eliminates such restriction on the amounts of methanol and water supplied to evaporating section 90. When step S220 is executed, the amounts of methanol and water supplied to the evaporator 90 are raised to the maximum amount that can be vaporized and heated by the combustion gas supplied to the evaporator 90.

By increasing the amounts of methanol and water supplied to the evaporating section 90, the evaporating section 90
Of the energy of the combustion gas supplied to the evaporator 90 increases in the evaporator 90 due to heat exchange. Therefore, the temperature of the flue gas discharged to the flue gas introduction section 94 decreases to about 50 to 90 ° C. The heat pipe 96 provided in the reforming section 92 has a structure for transmitting heat only in one direction as described above. When the amount of methanol and water introduced into the evaporating section 90 increases and the temperature of the combustion exhaust gas decreases, the inside of the reforming section 92 is sufficiently heated as described above. Heat exchange between the combustion exhaust gas and the reforming section 92 is not performed. In addition,
After the calorific value is no longer supplied from the flue gas,
The amount of heat required for the reforming reaction that progresses in the reforming section 92 is supplied from the above-described heater provided in the reforming section 92.

When the amounts of methanol and water supplied to the evaporating section 90 are changed in step S220, the three-way switching valve 37 is switched next (step S220).
230). As described above, until the inside of the reforming section 92 is sufficiently heated, the concentration of hydrogen in the fuel gas is insufficient.
4. Here, since it is determined in step S210 that the internal temperature of the reforming section 92 has sufficiently increased, the flow of the fuel gas is switched, and the supply of the fuel gas to the fuel cell 40 is started. Further, the supply of the oxidizing gas to the fuel cell 40 is started (step S240), and the present routine ends. The start of the supply of the oxidizing gas is executed by outputting a drive signal to the second flow regulator 83 provided in the second air supply path 77. As described above, when the supply of the fuel gas and the oxidizing gas to the fuel cell 40 is started, the electrochemical reaction in the fuel cell 40 becomes possible.

In the above description, the CO reduction unit 26
Although the confirmation of the operation status of step S230 is omitted, step S230
Prior to switching the three-way switching valve 37 to start supplying fuel gas to the fuel cell 40,
It may be confirmed that the CO reduction unit 26 is in a steady state. The temperature of the fuel gas detected by the third temperature sensor 62 provided in the third fuel supply passage 80 and the carbon monoxide in the fuel gas also detected by the carbon monoxide concentration sensor (not shown) provided in the third fuel supply passage 80 Based on concentration etc.
The operation state of the CO reduction unit 26 can be determined. In this way, after the CO reduction unit 26 is determined to be in the steady state and the CO reduction unit 26 confirms that the carbon monoxide concentration in the fuel gas can be sufficiently reduced, the three-way switching valve in step S230 Switching of 37 may be performed. In the above-described embodiment, the CO reduction unit 26 is configured to be in the steady state within the time until the fuel reformer 22 is in the steady state, and the operation of determining the operation state of the CO reduction unit 26 is performed. Omitted. Since the selective oxidation reaction of carbon monoxide in the CO reduction unit 26 is an exothermic reaction, the fuel gas containing hydrogen starts to be supplied from the fuel reformer 22 and the air tank 36
When a predetermined amount of compressed air is supplied from the above, the temperature in the CO reduction unit 26 rises with the progress of the exothermic oxidation reaction. Therefore, the CO reduction unit 26 can quickly raise the internal temperature to the predetermined temperature to bring the internal temperature into a steady state.

When the fuel gas and the oxidizing gas are supplied to the fuel cell 40 and the cell reaction is started, the fuel exhaust gas is discharged from the fuel cell 40 to the fuel exhaust gas passage 74. . This fuel exhaust gas is supplied to the burner 34 and used as fuel for a combustion reaction as described above. After the cell reaction in the fuel cell 40 is started, the fuel for the combustion reaction in the burner 34 is mainly fuel exhaust gas supplied through a fuel exhaust gas passage 74, and the shortage is supplied from the methanol tank 28. Supplemented with methanol.

When the cell reaction in the fuel cell 40 is started by executing the processing routine at the time of temperature increase shown in FIG. 5, thereafter, the fuel is supplied to the evaporating section 90 via the first fuel supply passage 78. The amount of methanol and water depends on the magnitude of the load connected to the fuel cell 40, that is, the fuel cell 4
It will change according to the amount of power generation required for zero. Thus, even when the amounts of methanol and water supplied to the evaporator 90 change, the temperature of the combustion gas generated in the burner 34 is monitored by the first temperature sensor 60,
The amount of methanol supplied from the methanol tank 28 to the burner 34 as the shortage described above is adjusted by the driving amount of the first pump 64, and the temperature of the combustion gas generated in the burner 34 is controlled. As a result, the amount of methanol and water supplied to the evaporator 90 is maintained at the maximum amount that can be vaporized and heated by the combustion gas generated in the burner 34 and discharged to the flue gas introduction unit 94. The temperature of the combustion exhaust gas to be kept is kept at 50 to 90 ° C.

According to the fuel cell system 20 of the present embodiment configured as described above, after the fuel reformer 22 has reached a steady state, the temperature of the combustion exhaust gas discharged from the evaporator 90 is reduced to about 50%. Since the temperature is up to 90 ° C., the amount of energy discharged from the fuel cell system 20 without being used is reduced, and it is possible to suppress the energy efficiency of the fuel cell system from being lowered by discarding the combustion exhaust gas. Since the steam reforming reaction that proceeds in the reforming section 92 of the fuel reforming apparatus 22 is an endothermic reaction, it is necessary to heat the inside of the reforming section 92 even after the fuel reforming apparatus 22 is in a steady state. In the embodiment, an electric heater is used as the heating means used in such a steady state. When the inside of the reforming section 92 is heated using a heater, energy is consumed by the heater and a predetermined amount of energy is discarded to the outside. However, when a heating unit such as a heater is used, the burner is not used. As compared with the case where the reforming section 92 is heated by the combustion gas, the amount of energy that is not used and discarded outside can be greatly reduced. According to the fuel cell system 20 of the present embodiment, even when the fuel reforming apparatus is in a steady state, the fuel reforming unit is heated by the combustion heat from the burner. Efficiency can be improved.

As described above, the fuel reformer 22 of this embodiment
Reduces the amount of energy that is not used and wasted when operating in steady state,
This has the effect of reducing the time required to reach a steady state at the time of starting. FIG. 6 shows the fuel reforming according to the present embodiment, which shows how the internal temperature of the reforming section (reforming catalyst temperature) rises and the amount of hydrogen generated in the fuel reformer increases when the fuel cell system is started. FIG. 9 is an explanatory diagram showing a result of a comparison between the device 22 and a conventionally known fuel reformer. In FIG. 6, the conventional fuel reformer is different from the conventional fuel reformer by the combustion heat of a burner attached to the fuel reformer.
This is a device that supplies heat required for temperature rise / vaporization of raw fuel and steam reforming reaction. In addition, a fuel reforming apparatus without an external heating means is a device without an external heating means such as a means for supplying combustion heat of a burner. Here, only an electric heater is provided in a reforming section. The fuel reformer was used.

As shown in FIG. 6 (A), the fuel reformer 22 of this embodiment has the capability of increasing the internal temperature (reforming catalyst temperature) of the reforming section to a predetermined temperature at the time of start-up (predetermined temperature). The time required to raise the temperature to the temperature can be said to be equivalent to that of the above-described conventional fuel reformer. That is, when the fuel reformer 22 is started, as described above, the reforming section 92 is rapidly heated by the high-temperature combustion exhaust gas generated by the combustion gas from the burner 34 via the heat exchange in the evaporating section 90. To be
It does not take a long time to raise the temperature inside the reforming section. On the other hand, in the case of a fuel reforming apparatus having no external heating means, the amount of heat generated by the heater provided in the reforming section is transferred to the inside of the reforming section by heat transfer, so that the temperature inside the reforming section rises. Takes a long time. When it takes time to raise the temperature inside the reforming section, the raw fuel gas once vaporized in the evaporating section provided prior to the reforming section cools down and condenses in the reforming section. Therefore, energy is consumed to vaporize the condensed raw fuel again, and even if heating is continued by the heater, the rise in temperature is temporarily stopped at a predetermined temperature (T0 in FIG. 6A). Further, it takes more time to sufficiently raise the temperature of the reforming section.

Further, as described above, since the ability to raise the internal temperature of the reforming section is sufficient, the fuel reformer 22 of this embodiment is required to generate a sufficient amount of hydrogen at the time of startup. It can be said that the time is short (Fig. 6
(B)). On the other hand, in the case of a fuel reforming apparatus having no external heating means, it takes time for the inside of the reforming section to rise in temperature as described above. Cost.

In the first embodiment, the compressor 32 is provided in the burner 34 and the compressed air is supplied from the compressor 32 to the air tank 36. However, the compressor 332 is provided in the burner 34. Instead, the combustion gas generated in the burner 34 may be directly introduced into the fuel reformer 22. When the compressor 32 is not provided with the burner 34, a compressor for obtaining compressed air may be provided independently of the burner 34. Further, a configuration may be adopted in which the compressed air is temporarily stored in the air tank 36 and the air taken in from the outside is pressurized and supplied directly to the fuel cell 40.

In the first embodiment, the directional heat exchange means is provided between the reforming section 92 and the flue gas introducing section 94, so that the heat is only supplied from the flue gas side to the reforming section side at the time of starting. Although it is configured to be transportable, the above-described one-way heat transport can also be performed by making the flow path of the combustion exhaust gas switchable without providing such heat exchange means. Hereinafter, such a configuration will be described as a second embodiment. FIG. 7 shows a fuel reformer 22 according to the second embodiment.
It is explanatory drawing showing the outline of a structure of a. Fuel reformer 2
Reference numeral 2a denotes a fuel reforming apparatus provided in a fuel cell system similar to the fuel cell system 20 of the first embodiment. In the following description, members common to the fuel cell system 20 of the first embodiment have the same reference numerals. Will be appended. Further, among the members constituting the fuel reformer 22a of the second embodiment shown in FIG. 7, members having the same functions as the members of the fuel reformer 22 of the first embodiment include fuel reformers. The member numbers in the device 22 are denoted by reference characters a.

The fuel reformer 22a has an evaporator 90a and a reformer 92a. The evaporator 90a has a burner 34a
The combustion gas generated by the combustion reaction in the burner 34a is introduced into the inside of the evaporator 90a. Also,
The first fuel supply passage 78 is connected to the evaporating section 90a, so that methanol and water can be supplied from the methanol tank 28 and the water tank 30. The first fuel supply path 78 forms a heat exchange section in the evaporating section 90a, and methanol and water in the first fuel supply path 78
By performing heat exchange with the combustion gas supplied from the burner 34a, the temperature is raised and vaporized to become a fuel gas.

The first fuel supply passage 78 becomes a fuel gas passage 88 after forming the heat exchange section, and is connected to the reforming section 92a. The raw fuel gas supplied to the reforming section 92a via the fuel gas passage 88 is subjected to a steam reforming reaction in the reforming section 92a. The reforming section 92a includes the reforming section 9 of the first embodiment.
As in the case of No. 2, pellets made of a reforming catalyst are filled. The reformed gas generated by the reforming reaction in the reforming section 92a is discharged to the second fuel supply path 79 connected to the reforming section 92 and supplied to the CO reduction section 26. In addition,
The reforming section 92a includes a heater (not shown) similarly to the reforming section 92 of the first embodiment, and when operating in a steady state, the energy required for the reforming reaction is reduced by the heat energy supplied from the heater. I am covering. Further, the reforming section 92a includes a fifth temperature sensor 85 therein. The fifth temperature sensor 85 is connected to the control unit 50, and can input information on the temperature inside the reforming unit 92a to the control unit 50.

The combustion gas having exchanged heat with methanol and water in the evaporating section 90a is discharged to a combustion exhaust gas pipe 95 as combustion exhaust gas. This flue gas pipe 9
5, a switching valve 87 is provided.
By switching 7, the flow path of the combustion exhaust gas can be switched in two ways as described below. A flue gas introducing portion 94a is provided on an outer peripheral portion of the reforming portion 92a.
a can be introduced. Combustion exhaust gas introduction part 94a
The combustion exhaust gas introduced therein exchanges heat with the reforming section 92a. Therefore, if the combustion exhaust gas has a higher temperature than the reforming section 92a, the reforming section 92a can be heated by such heat exchange with the combustion exhaust gas. The flue gas that has passed through the flue gas introducing portion 94a is discharged outside the fuel cell system.

On the other hand, when the switching valve 87 is switched to a state different from the above, the combustion exhaust gas is discharged to the outside of the combustion cell system without exchanging heat with the reforming section 92a. The combustion exhaust gas pipe 95 is provided with a sixth temperature sensor 86 upstream of the switching valve 87. The sixth temperature sensor 86 is connected to the control unit 50 and outputs information on the temperature of the combustion exhaust gas to the control unit 5.
0 can be input. The control unit 50 controls the switching valve 87 based on the information on the combustion exhaust gas temperature.
To output a drive signal to control the connection state of the flow path. In this embodiment, an electromagnetically operated valve is used as the switching valve 87, but a different type of valve such as a motor operated valve or an air operated valve may be used.

In the fuel cell system provided with the fuel reformer 22a of the second embodiment, at the time of startup, the same processing as the startup processing routine of the first embodiment shown in FIG. 4 is performed. Here, in the second embodiment, as a process executed at the time of startup, when the combustion reaction of the burner is started in step S140 in the startup process routine of FIG. It is to be introduced into the combustion exhaust gas introduction section 94a on the reforming section 92a side. As a result, when the fuel cell system including the fuel reformer 22a is started, the combustion gas generated in the burner 34a is introduced into the combustion exhaust gas introduction section 94a. Here, similarly to the first embodiment, step S170
When the supply of methanol and water to the evaporating section 90a is started by the
Is limited to one-third to two-thirds of the amount that can be vaporized and raised by the combustion gas supplied from the combustion gas, the combustion exhaust gas introduced into the combustion exhaust gas introduction portion 94a is 300 to 500.
As a result, the temperature of the reforming portion 92a is rapidly increased.

Further, in the fuel cell system including the fuel reforming apparatus 22a of the second embodiment, after startup, processing similar to the processing routine at the time of temperature increase shown in FIG. 5 is executed. FIG. 8 is a flowchart illustrating a temperature-raising processing routine executed after the fuel cell system according to the second embodiment is started. This routine is executed by the CPU 54 after the above-described processing routine at the time of starting is completed. When this routine is started, first, the CPU 54 sets the fifth temperature sensor 8
5, the temperature t4 inside the reforming section 92a measured is read (step S300). Next, the state of the internal temperature of the reforming section 92a is determined by comparing the temperature t4 inside the reforming section 92a with a predetermined reference value t5 (step S31).
0).

The predetermined reference value t5 is the value of the reforming section 92a
This is a predetermined value as the minimum value of the temperature in the reforming section when the steam reforming reaction can proceed with sufficient efficiency on the catalyst surface provided in. When the internal temperature t4 of the reforming section 92a is lower than the predetermined reference value t5, step S300
The process of reading the temperature t4 inside the reforming section 92a and comparing it with the reference value t5 is repeated until the temperature inside the reforming section 92 rises sufficiently. At this time, the combustion exhaust gas introduction portion 94a provided on the outer peripheral portion of the reforming portion 92a.
As described above, since the high-temperature flue gas is introduced through the flue gas pipe 95 and the switching valve 87, the internal temperature of the reforming section 92a is rapidly rising.

In step S310, the reforming section 92a
When the internal temperature t4 becomes equal to or higher than the reference value t5, it is determined that the internal temperature of the reforming section 92a has risen to an extent that a sufficient amount of hydrogen can be generated by the reforming reaction. The amounts of methanol and water to be supplied to 90a are changed (Step S320). That is, the restriction on the drive amount of the second pump 65 and the third pump 66 is stopped. In the fuel reforming apparatus 22a of the present embodiment, similarly to the fuel reforming apparatus 22 of the above-described first embodiment, the amount of heat generated by the burner 34a at the time of startup is maintained at a predetermined value, and the evaporating section 90a Is reduced to one third to two thirds of the amount that can be sufficiently vaporized and heated by the combustion gas supplied from the burner 34a. Executing step S320 eliminates such restriction on the amount of methanol and water supplied to evaporating section 90a. When step S320 is executed, the amounts of methanol and water supplied to the evaporator 90a are increased to about the maximum amount that can be vaporized and heated by the combustion gas supplied to the evaporator 90a.

By increasing the amounts of methanol and water supplied to the evaporator 90a, the evaporator 9
Of the energy of the combustion gas supplied to Oa, the proportion consumed by heat exchange in evaporator 90a increases. Therefore, the temperature of the flue gas discharged to the flue gas introduction portion 94a gradually decreases.

Next, the temperature t6 of the flue gas is read from the sixth temperature sensor 86 (step S330), and the temperature t6 of the flue gas is compared with a predetermined reference value t7 (step S340). Here, the predetermined reference value t7 is a value that has been determined in advance as the temperature of the combustion exhaust gas when the temperature has decreased to such an extent that a sufficient amount of heat cannot be transmitted to the reforming section 92a. When the temperature t6 of the combustion exhaust gas is equal to or higher than the predetermined reference value t7, the process returns to step S330,
Until the temperature of the flue gas falls below the predetermined temperature, the above-described processing of reading the temperature t6 of the flue gas and comparing it with the reference value t7 is repeated.

In step S340, when the temperature t6 of the flue gas falls below the predetermined reference value t7,
Next, the switching valve 87 is switched (step S35).
0), the flow path of the combustion exhaust gas is changed. Switching valve 87
, The flue gas introduced into the flue gas introduction portion 94a is discharged to the outside. The introduction of the flue gas into the flue gas introducing portion 94a is stopped, and the reforming portion 92
After the supply of the heat quantity to the reforming section 92a is stopped, the heat quantity required for the reforming reaction progressing in the reforming section 92a becomes the reforming section 9a.
2a is supplied from the heater described above.

Thereafter, the three-way switching valve 37 is switched (step S360) to switch the state in which the fuel gas discharged from the CO reduction unit 26 is supplied to the burner 34 to the state in which the fuel gas is supplied to the fuel cell 40. Further, a drive signal is output to the second flow regulator 83 to start supplying the oxidizing gas to the fuel cell 40 (step S370), and the present routine ends. As a result, in the fuel cell 40, power generation is started by an electrochemical reaction.

When the cell reaction in the fuel cell 40 is started by executing the temperature raising routine shown in FIG. 8, the control of the amount of methanol and water supplied to the evaporating section 90a is then performed. The control regarding the temperature of the combustion gas generated in the burner 34a is performed in the same manner as in the first embodiment described above. That is, the amounts of methanol and water supplied to the evaporating section 90a change according to the magnitude of the load connected to the fuel cell 40, and the temperature of the combustion gas generated in the burner 34a depends on the driving amount of the first pump 64. By adjusting the temperature, a predetermined relationship is maintained between the amounts of methanol and water, whereby the temperature of the flue gas discharged to the flue gas pipe 95 is maintained at 50 to 90 ° C. In the fuel reformer 22a of this embodiment, the flue gas introducing section 9 provided on the outer periphery of the reforming section 92a is provided.
It is also preferable to provide a predetermined fin structure or the like in 4a to increase the efficiency of transmitting the heat of the combustion exhaust gas to the reforming section 92a.

According to the fuel cell system including the fuel reformer 22a of the second embodiment configured as described above, the same effects as those of the fuel cell system 20 of the first embodiment can be obtained. That is, at the time of startup, the reforming section 92a is rapidly heated by the high-temperature combustion exhaust gas.
The temperature inside a can be quickly brought close to the steady state. Further, after the fuel reformer 22a enters a steady state, the rate of heat consumed by heat exchange with methanol and water in the evaporator 90a is increased to lower the temperature of the flue gas and to reduce the flow rate of the flue gas. Switch. Therefore, it is possible to reduce the amount of energy that is discarded from the fuel reformer 22a after the temperature of the reforming section 92a is sufficiently raised, and it is possible to sufficiently increase the energy efficiency of the entire system. By using the fuel cell system including the fuel reforming device 22a of the present embodiment, similarly to the fuel cell system 20 of the first embodiment, the reformer is heated by the burner combustion gas even during steady operation. Energy efficiency can be improved by about 10% as compared with the case where a fuel reformer is used.

Further, the fuel reformer 22a of the second embodiment
According to the third embodiment, the following effects are obtained in addition to the effects common to the first embodiment. That is, the reforming unit 92
a, the flue gas introduction portion 94a is provided around
When the inside of the reforming section 92a is in a steady state, the combustion exhaust gas introduction section 94a functions as a heat insulating material,
The heat radiation from the reforming section 92a can be suppressed, and the energy efficiency can be further improved.

In the second embodiment described above, the evaporator 90
a and the reforming section 92a are formed separately, and the flow path of the combustion exhaust gas discharged from the evaporating section 90a is switched to form the reforming section 92a.
However, the configuration may be such that the evaporating section and the reforming section are integrally formed so that the flow path of the combustion exhaust gas can be switched. Hereinafter, such a configuration will be described as a third embodiment.

FIG. 9 shows a fuel reformer 22b according to the third embodiment.
FIG. 3 is an explanatory diagram showing an outline of the configuration of FIG. Fuel reformer 22b
Is a fuel reforming apparatus provided in a fuel cell system similar to the fuel cell system 20 of the first embodiment. In the following description, members common to the fuel cell system 20 of the first embodiment are denoted by the same reference numerals. I will attach it. Further, among the members constituting the fuel reformer 22b of the third embodiment shown in FIG.
The members having the same functions as the members included in the fuel reforming apparatus 22 of the first embodiment are indicated by the reference numbers b in the member numbers of the fuel reforming apparatus 22.

The fuel reformer 22b includes an evaporator 90b and a reformer 9 whose longitudinal direction is the direction in which the raw fuel gas passes.
2b, the fuel reformer 22b according to the third embodiment.
Here, the evaporating section 90b and the reforming section 92b are integrally formed, and a plurality of reforming sections 92b are arranged around the evaporating section 90b in a state parallel to the evaporating section 90b. Evaporator 90b
As in the above-described embodiment, a burner 34b is provided and a first fuel supply path 78 is connected, and the first fuel supply path forms a heat exchange section in the evaporating section 90b. . Therefore, the methanol and water supplied via the first fuel supply passage 78 are heated and vaporized by heat exchange with the combustion gas supplied from the burner 34b to become fuel gas.

The reforming section 9 formed around the evaporating section 90b
2b has a first fuel supply passage 78 via an evaporator 90b.
Connect. The methanol and water vaporized and heated in the evaporator 90b are supplied to the reformer 92b and subjected to a steam reforming reaction. The reforming section 92b is filled with pellets made of a reforming catalyst as in the above-described embodiment. The reformed gas generated by the reforming reaction in the reforming section 92b is discharged to the second fuel supply path 79 via a predetermined flow path connected to the reforming section 92b and supplied to the CO reduction section 26. . The reforming section 92b includes a heater (not shown) as in the above-described embodiment, and when operating in a steady state, the energy required for the reforming reaction is covered by the heat energy supplied from the heater. I have.

The combustion gas that has exchanged heat with methanol and water in the evaporating section 90b is discharged as combustion exhaust gas to the outside of the fuel reformer 22b, and may take two types of flow paths along the way. . Here, an electromagnetic valve 89 is provided in a flow path for directly discharging the combustion exhaust gas from the evaporator 90b to the outside of the fuel reformer 22b. The solenoid-operated valve 89 is connected to the control unit 50, and the open / close state of the valve is controlled by the control unit 50.

Further, in addition to the above-mentioned electromagnetically operated valve 89, a pressure release valve 9 is provided in the flow path of the combustion gas in the evaporating section 90b.
1 is provided. Each of the reforming sections 92b provided around the evaporating section 90b is provided with a combustion exhaust gas introducing section 94b covering the outer periphery thereof.
Are provided at a plurality of locations in the evaporating section 90b where the combustion gas flow path and the combustion exhaust gas introduction section 94b are connected. The pressure release valve 91 is provided with a spring, and is opened when the pressure in the combustion gas flow path in the evaporating section 90b exceeds a predetermined value. When the pressure release valve is opened, the combustion exhaust gas flows from the evaporating section 90b side to the combustion exhaust gas introduction section 94b.
And the flue gas introduced is
Combustion exhaust gas introduction section 9 provided on the outer periphery of reforming section 92b
The fuel gas passes through the inside of the fuel reformer 4b and is discharged to the outside of the fuel reformer 22b. At this time, when the temperature of the combustion exhaust gas is different from the internal temperature of the reforming section 92b, heat exchange is performed between the combustion exhaust gas and the reforming section 92b. Note that the above-mentioned solenoid operated valve 89
May be a motor operated type or an air operated type instead of the electromagnetically operated type.

In the fuel cell system provided with the fuel reforming apparatus 22b of the third embodiment, at the time of startup, the same processing as the startup processing routine of the first embodiment shown in FIG. 4 is performed. Here, in the third embodiment, a drive signal is output to the solenoid-operated valve 89 when the combustion reaction of the burner is started in step S140 in the startup processing routine of FIG. The electromagnetic valve 89 is closed. By performing such processing, when the fuel cell system including the fuel reformer 22b is started, the pressure inside the evaporator 90b becomes equal to or higher than a predetermined value due to the combustion gas generated by the burner 34b, and the pressure release valve 91 is turned on. When the combustion exhaust gas is opened, the combustion exhaust gas
4b. At this time, similarly to the above-described embodiment, the evaporating section 90 is provided through the first fuel supply passage 78.
Since the amounts of methanol and water supplied to b are reduced, the flue gas introduced into the flue gas inlet 94b has a high temperature of 300 to 500 ° C. Therefore, by performing heat exchange with the high-temperature combustion exhaust gas, the reforming section 92b is rapidly heated.

Further, in the fuel cell system including the fuel reformer 22b of the third embodiment, after startup, processing similar to the processing routine at the time of temperature increase shown in FIG. 5 is executed. FIG. 10 is a flowchart illustrating a heating-time processing routine that is executed after the fuel cell system according to the third embodiment is started. This routine is executed by the CPU 54 after the above-described processing routine at the time of starting is completed. When this routine is started, first, the CPU 54 reads the temperature t2 of the reformed gas measured by the second temperature sensor 61 (step S400). Next, the state of the internal temperature of the reforming section 92b is determined by comparing the temperature t2 of the reformed gas with a predetermined reference value t3 (step S410).

The predetermined reference value t3 is the same as the predetermined reference value t3 in the processing routine at the time of temperature rise in the first embodiment, and is sufficient for the steam reforming reaction on the catalyst surface provided in the reforming section 92b. This is a predetermined value as the minimum value of the temperature of the reformed gas when the process can proceed with efficiency. When the temperature t2 of the reformed gas is lower than the predetermined reference value t3, the process returns to step S400, and the reading of the temperature t2 of the reformed gas and the comparison with the reference value t3 until the temperature inside the reforming section sufficiently rises. Repeat the comparison process. At this time, the high-temperature combustion exhaust gas is introduced into the combustion exhaust gas introduction portion 94b provided on the outer peripheral portion of the reforming portion 92b through the pressure release valve 91 as described above. 92b
The internal temperature is rising rapidly.

In step S410, when the temperature t2 of the reformed gas is equal to or higher than the reference value t3, the internal temperature of the reforming section 92b is raised to such an extent that a sufficient amount of hydrogen can be generated by the reforming reaction. Then, the amounts of methanol and water supplied to the evaporating section 90b are changed (step S420). That is, the restriction on the drive amount of the second pump 65 and the third pump 66 is stopped. In the fuel reformer 22b of the present embodiment, similarly to the above-described embodiment, the amount of heat generated by the burner 34b at the time of startup is maintained at a predetermined value, and methanol and water supplied to the evaporator 90b are maintained. The amount is reduced to one third to two thirds of the amount that can be sufficiently vaporized and heated by the combustion gas supplied from the burner 34b. This step S42
By performing 0, such a restriction on the amounts of methanol and water supplied to the evaporating section 90b is not performed. When step S420 is executed, the amounts of methanol and water supplied to the evaporator 90b are raised to about the maximum amount that can be vaporized and heated by the combustion gas supplied to the evaporator 90b.

By increasing the amounts of methanol and water supplied to the evaporator 90b, the evaporator 9
Of the energy of the combustion gas supplied to Ob, the proportion consumed by heat exchange in the evaporator 90b increases. Therefore, the temperature of the flue gas discharged to the flue gas introduction portion 94b gradually decreases.

Next, a drive signal is output to the solenoid-operated valve 89 to open the solenoid-operated valve 89 (step S4).
30). When the electromagnetic valve 89 is opened, the combustion exhaust gas is discharged to the outside of the fuel reformer 22b via the electromagnetic valve 89. At the same time, the pressure in the flue gas passage in the evaporating section 90b decreases, and the pressure release valve 9
1 is closed. When the pressure release valve 91 is closed,
The supply of the combustion exhaust gas to the combustion exhaust gas introduction unit 94b is stopped, and the heat exchange between the combustion exhaust gas and the reforming unit 92b is not performed.

Thereafter, the three-way switching valve 37 is switched (step S440) to switch the state in which the fuel gas discharged from the CO reduction unit 26 is supplied to the burner 34 to the state in which the fuel gas is supplied to the fuel cell 40. Further, a drive signal is output to the second flow regulator 83 to start supplying the oxidizing gas to the fuel cell 40 (step S450), and the present routine ends. As a result, in the fuel cell 40, power generation is started by an electrochemical reaction.

When the cell reaction in the fuel cell 40 is started by executing the temperature raising routine shown in FIG. 10, the control of the amounts of methanol and water supplied to the evaporating section 90b is then performed. The control regarding the temperature of the combustion gas generated in the burner 34b is performed in the same manner as in the above-described embodiment. That is, the amounts of methanol and water supplied to the evaporating section 90b change according to the magnitude of the load connected to the fuel cell 40, and the temperature of the combustion gas generated in the burner 34b depends on the driving amount of the first pump 64. By adjusting the temperature, a predetermined relationship is maintained between the amounts of methanol and water, whereby the temperature of the combustion exhaust gas discharged from the evaporating section 90b is maintained at 50 to 90 ° C.

In the fuel reformer 22b of the third embodiment, the pressure in the evaporator 90b is adjusted by the electromagnetically operated valve 89 to operate the pressure release valve 91 for switching the flow path of the combustion exhaust gas. However, a thermally operated valve may be used instead of the electromagnetically operated valve 89. Such a configuration is described below as a fourth embodiment.

FIG. 11 shows a fuel reformer 22 according to the fourth embodiment.
It is explanatory drawing which shows the outline of a structure of c. Fuel reformer 22
c denotes a fuel reformer provided in a fuel cell system similar to the fuel cell system 20 of the first embodiment. In the following description, members common to those of the fuel cell system 20 of the first embodiment have the same numbers. Will be appended. Further, among the members constituting the fuel reformer 22c of the 43rd embodiment shown in FIG. 11, members having the same functions as the members provided in the fuel reformer 22 of the first embodiment include fuel reformers. The member number in the device 22 is represented by adding a symbol c.

The fuel reforming device 22c includes an evaporator 90c and a reformer 92c, similarly to the fuel reformer 22b of the third embodiment.
Are integrally formed, and a plurality of reforming sections 92c are provided around the evaporating section 90c. Note that in FIG.
c is shown only partially. The fuel reformer 22c according to the fourth embodiment has a configuration similar to that of the fuel reformer 22b according to the third embodiment, and the combustion exhaust gas discharged from the evaporator 90c passes through the pressure release valve 91. The fuel gas can be introduced into the flue gas introduction portion 94c. When the high-temperature flue gas is introduced into the flue gas introduction portion 94c, the temperature of the reforming portion 92c is raised by the calorific value of the flue gas.

On the other hand, the fuel reformer 22c of the fourth embodiment
Has a thermally operated valve 89c instead of the electromagnetically operated valve 89 included in the fuel reformer 22b of the third embodiment. The thermally actuated valve 89c is made of a bimetal or a shape memory alloy, and is a valve body that closes at a high temperature exceeding about 150 ° C. and opens at a low temperature of about 150 ° C. or less. Therefore, when the temperature of the combustion exhaust gas that has undergone heat exchange in the evaporator 90c becomes the above-described high temperature, the heat operated valve 89c is closed and the pressure in the evaporator 90c is increased, whereby the pressure release valve 91c is opened. Become. At this time, the combustion exhaust gas is introduced into the combustion exhaust gas introduction portion 94c via the pressure release valve 91c and then discharged out of the fuel reforming device 22c. The reforming portion 92c exchanges heat with the combustion exhaust gas. Raise the temperature. Further, when the temperature of the combustion exhaust gas that has undergone heat exchange in the evaporator 90c becomes the low temperature, the heat operation valve 89c is opened, and the combustion exhaust gas is discharged from the heat operation valve 89c.
c to the outside of the fuel reformer 22c,
The pressure in 0c drops. At the same time, pressure release valve 91c
Is closed, and the supply of the combustion exhaust gas to the combustion exhaust gas introduction unit 94c is stopped.

In the fuel cell system provided with the fuel reforming apparatus 22c of the fourth embodiment, at the time of startup, the same processing as the startup processing routine of the first embodiment shown in FIG. 4 is performed. Here, when the combustion reaction of the burner 34c is started as an operation corresponding to step S140 in the start-time processing routine of FIG.
Since the amounts of methanol and water supplied to the evaporator 90c via the fuel supply passage 78 are suppressed, the amount of combustion exhaust gas discharged from the evaporator 90c is 30%.
The temperature is as high as 0 to 500 ° C. Therefore, the thermally actuated valve 8
9c is closed, and the pressure release valve 91c is open, so that high-temperature combustion exhaust gas is introduced into the combustion exhaust gas introduction section 94c. By performing heat exchange with the high-temperature combustion exhaust gas, the reforming section 92c is rapidly heated.

Further, in the fuel cell system including the fuel reforming apparatus 22c of the fourth embodiment, after startup, the same processing as the processing routine at the time of temperature increase shown in FIG. 5 is executed. Here, step S22 in the temperature raising processing routine of FIG.
As an operation corresponding to 0, the restriction on the amounts of methanol and water supplied to the evaporating section 90c is stopped, and the evaporating section 9c is stopped.
0c is supplied to the evaporator 90
The temperature is raised to about the maximum amount that can be vaporized and heated by the combustion gas supplied to c. As described above, when the amounts of methanol and water supplied to the evaporating unit 90c are increased, the temperature of the combustion exhaust gas discharged from the evaporating unit 90c decreases, and the heat operation valve 89c is opened to open the pressure release valve 91c.
Is closed. Therefore, the combustion exhaust gas is discharged to the outside of the fuel reforming device 22c without being introduced into the combustion exhaust gas introduction section 94c.

Further, the fuel cell 40
Starts the battery reaction in the evaporator 90.
The control of the amount of methanol and water supplied to c and the temperature of the combustion gas generated in the burner 34c are as follows.
This is performed in the same manner as in the previously described embodiment. Therefore, the temperature of the combustion exhaust gas discharged from the evaporating section 90c to the outside of the fuel reformer 22c is kept at 50 to 90 ° C.

The fuel reformer 22b according to the third embodiment and the fuel reformer 22c according to the fourth embodiment, which are configured as described above, are used.
According to the fuel cell system including the above, the same effect as the fuel cell system 20 of the first embodiment can be obtained. That is, since the reforming section is rapidly heated by the high-temperature combustion exhaust gas at the time of starting, the internal temperature of the reforming section can be quickly brought close to the steady state. After the fuel reformer enters the steady state, the amount of heat consumed by heat exchange with methanol and water in the evaporator is increased, the temperature of the flue gas is reduced, and the flow path of the flue gas is switched. Therefore, it is possible to reduce the amount of energy that is discarded from the fuel reformer after the temperature of the reforming section has sufficiently increased, and it is possible to sufficiently increase the energy efficiency of the entire system. By using the fuel cell system including the fuel reforming apparatuses of the third and fourth embodiments, the reformer is heated by the combustion gas of the burner even during steady operation, similarly to the fuel cell system 20 of the first embodiment. The energy efficiency can be improved by about 10% as compared with the case where a conventionally known fuel reformer is used.

According to the fuel reforming apparatus 22b of the third embodiment and the fuel reforming apparatus 22c of the fourth embodiment, the following effects can be obtained, similarly to the fuel reforming apparatus 22a of the second embodiment. Play. In other words, since the flue gas introduction section is provided around the reforming section, when the inside of the reforming section is in a steady state, the combustion exhaust gas introduction section functions as a heat insulating material, and the heat release from the reforming section is reduced. And energy efficiency can be further improved. Further, the evaporating sections 90b, 90
In FIG. 9C, since the flows of the combustion gas and the raw fuel are reversed as shown in FIGS. 9 and 11, the heat exchange efficiency is further improved.

Further, in the fuel reformer 22b of the third embodiment and the fuel reformer 22c of the fourth embodiment, a pressure release valve and a thermally actuated valve are provided in the flow path of the combustion exhaust gas supplied from the burner. Since the flow path of the combustion exhaust gas is controlled, the configuration of the fuel reformer can be simplified.
That is, after inputting the fuel exhaust gas and the temperature of the reforming section,
It is not necessary to determine the timing of opening and closing a predetermined valve element and to output a drive signal to the predetermined valve element as necessary to open and close the valve element, and output a drive signal to a predetermined valve element. No electrical wiring or temperature sensor is required.

The type of valve provided at the connection between the evaporator and the flue gas introduction part and the type of valve provided at the flow path for discharging the combustion exhaust gas directly from the evaporator to the outside are as described in the third and fourth embodiments. The present invention is not limited to the combination shown in the example, and when the fuel reformer is started and at the time of transition from the start to the steady state, if the flow path of the combustion exhaust gas can be changed as described above, May use different types of valve bodies. In the third embodiment, an electromagnetic valve and a pressure release valve are used, and in the fourth embodiment, a heat valve and a pressure release valve are used.
Each valve element can be designed to be replaced with a different type of valve element.

In the first, third, and fourth embodiments described above, the determination of the temperature rise state of the reforming section is made based on the temperature of the reformed gas detected by the second temperature sensor 61. In the second embodiment, the determination is made based on the internal temperature of the reforming section measured by the fifth temperature sensor 85. The temperature may be based on the temperature of the reformed gas, and may be based on the temperature that well reflects the internal temperature of the reforming section.

Further, in each of the above-described embodiments, the reforming section of each fuel reforming apparatus is configured to fill the inside with the pellet made of the reforming catalyst. Alternatively, the reforming section may be constituted by a honeycomb. That is, the reforming reaction can be advanced by carrying the reforming catalyst on the surface of the honeycomb and passing the raw fuel gas through such a honeycomb surface. The honeycomb supporting the catalyst, such as coating a metal honeycomb surface with alumina, further applying a catalyst metal to the surface, or adding a binder to a crushed catalyst pellet described above and applying a binder to the honeycomb surface, etc. Can be created by any method. When the reforming unit is configured by a honeycomb, as a method of heating the reforming unit after the fuel reforming device is in a steady state, the metal honeycomb itself is energized to cause the catalyst supported on the surface to be heated. Since direct heating can be performed, efficiency during heating can be increased.

In each of the above-described embodiments, the reforming reaction proceeding in the reforming section is based on the steam reforming reaction represented by the equations (4) to (6). An oxidation reforming reaction may be performed. Hereinafter, the partial oxidation reforming reaction will be described.

CH ₃ OH + (１ ／) O ₂ → CO ₂ + 2H ₂ +189.5 (kJ / mol) (7)

When a Cu—Zn catalyst is used as a reforming catalyst, as in the reforming section in each of the above-described embodiments, oxygen is added to the raw fuel gas and supplied to the reforming section. In the section, the exothermic reaction represented by the equation (7) continues to proceed until the added oxygen is consumed and disappears. Of course,
While the exothermic reaction shown in the equation (7) is proceeding, the ordinary steam reforming reaction shown in the equation (6) is performed. After the oxygen is consumed and the exothermic reaction shown in the equation (7) is no longer performed, only the reforming reaction involving endotherm shown in the equation (6) is performed. In this way, by adding oxygen to the raw fuel gas and supplying it to the reforming section and allowing the oxidative reforming reaction involving heat to proceed in the reforming section, it is possible to cover the calorie required for the steam reforming reaction. . When both the steam reforming reaction and the oxidative reforming reaction are performed in the reforming section in this manner, both reactions may be promoted by the same catalyst as described above, or the respective reforming reactions may be performed. Alternatively, different catalysts may be prepared.

FIG. 12 is a system similar to the fuel cell system 20 of the first embodiment, and has a configuration of a fuel cell system 20d including a fuel reforming apparatus for performing a partial oxidation reforming reaction in addition to a steam reforming reaction. It is explanatory drawing which illustrates the outline of. The fuel cell system 20 d
Therefore, the same reference numerals are given to the common members. In the fuel cell system 20d, the first supply of compressed air from the air tank 36 to the burner 34 is performed.
An air supply branch 93 is provided, branching from the air supply path 76. The air supply branch passage 93 is connected to the first fuel supply passage 78, and can supply compressed air to methanol and water passing through the first fuel supply passage 78. In addition, a fourth flow rate regulator 97 is provided in the air supply branch 93 so that the amount of compressed air supplied through the air supply branch 93 can be adjusted. The fourth flow regulator 97 is connected to the control unit 50 and is driven by the control unit 50. The control unit 50 determines the amount of oxygen required for the oxidation reforming reaction, and controls the driving amount of the fourth flow regulator 97.

As described above, the fuel cell system 2
At 0d, oxygen added to the raw fuel gas is obtained from compressed air supplied from an air tank. The amount of the oxidative reforming reaction that proceeds in the reforming section can be controlled by adjusting the amount of compressed air supplied from the air tank. By adjusting the amount of raw fuel supplied to the reforming section and the amount of compressed air added to the raw fuel, the amount of heat required for the steam reforming reaction proceeding in the reforming section and the oxidation reforming proceeding in the reforming section are improved. The amount of heat generated in the reaction can be balanced, and the energy efficiency can be improved. With such a configuration, the reforming reaction can proceed without providing a heating means such as a heater in the reforming section as in the above-described embodiment. Due to the high temperature of the reforming section, the amount of oxygen in the compressed air introduced into the reforming section is introduced into the reforming section even when considering the heat loss, which dissipates the generated heat to the outside of the reforming section. When the amount of methanol is 10 to 20% of the amount of methanol, the endothermic and the exothermic accompanying the reaction can be balanced.

As described above, when the steam reforming reaction is performed by using the heat generated in the oxidation reforming reaction instead of providing the heater in the reforming section, the steam reforming reaction is performed while heating with the heater. Energy efficiency is further improved. The fuel reformer of each of the above-described embodiments having a heater in the reforming section has about 10% higher energy efficiency than the conventional fuel reformer in which the reforming section is heated by the combustion gas from the burner even in a steady state. However, if the fuel reformer of each of the above embodiments is configured to utilize the heat generated by the oxidation reforming reaction instead of the heater, the energy efficiency is improved by about 15% as compared with the conventional fuel reformer. Can be done.

In the above-described embodiment, the burner for supplying the combustion gas to the evaporator is a combustion device having an ignition device. However, the burner may be another type of device such as a combustion device having an oxidation catalyst. It is sufficient if a predetermined high-temperature gas can be generated.

In the embodiment described above, methanol is used as a raw fuel for obtaining a hydrogen-rich fuel gas, but other types of hydrocarbons can be used as the raw fuel. If the fuel reforming apparatus is provided with an evaporating unit and includes a step of generating a raw fuel gas heated to a predetermined temperature by the combustion gas from the burner, the effects described above can be obtained by applying the present invention. . Examples of applicable raw fuels other than methanol include methane, natural gas, ethane, propane, butane, gasoline, light oil, ethanol, acetone, and DME.
(Dimethyl ether).

Here, when a gaseous raw fuel such as methane is used as the raw fuel, it is not necessary to vaporize the raw fuel.
Since it is desirable to raise the temperature of the raw fuel before supplying it to the fuel reformer, it is necessary to supply both the water and the gaseous raw fuel required for the steam reforming reaction to the fuel reformer. Thus, the temperature of the gaseous raw fuel can be raised simultaneously with the vaporization of water. As a method for supplying water and gaseous raw fuel to the fuel reformer, water and gaseous raw fuel may be mixed beforehand and then supplied to the fuel reformer, or water and gaseous raw fuel may be supplied. The fuel may be separately supplied to the fuel reformer.

Further, it is not always necessary to carry out a steam reforming reaction in the reforming section, and a reformed gas may be generated only by an oxidation reforming reaction using a liquid raw fuel such as methanol. Even in such a case, after the fuel reforming device is in a steady state, it is possible to vaporize the liquid raw fuel or the liquid raw fuel containing oxygen required for the oxidation reforming reaction and sufficiently raise the temperature. Since the amount of heat that can be supplied may be supplied by the burner, the configuration of the above-described embodiment can be applied.

In the above-described embodiment, the fuel cell to which the fuel gas obtained by reforming the raw fuel by the fuel reformer is supplied is a polymer electrolyte fuel cell. The fuel cell system may include the fuel reformer described above. In particular, when a phosphoric acid fuel cell or a solid oxide fuel cell is used as the fuel cell, the configuration of the fuel cell system of the above-described embodiment can be applied mutatis mutandis.

In the fuel cell system described above, the amount of the reformed gas generated by the fuel reformer is changed in accordance with the change in the load connected to the fuel cell 40. The reformed gas generated by the apparatus or the hydrogen gas separated from the reformed gas may be temporarily stored, and the stored reformed gas or hydrogen gas may be supplied to the fuel cell. In such a case, the reforming reaction can always proceed with good efficiency while keeping the rate of generating the reformed gas constant. In the fuel reformer having such a configuration, after reaching a steady state, the amount of the raw fuel and the like supplied to the evaporator is reduced to about the maximum amount that can be vaporized and heated by the combustion gas supplied from the burner. As a result, a sufficient amount of reformed gas can be generated stably, and the amount of energy that is not used in the fuel reformer and discarded can be reduced.

The embodiments of the present invention have been described above.
The present invention is not limited to such embodiments at all, and it goes without saying that the present invention can be implemented in various modes without departing from the gist of the present invention.

[Brief description of the drawings]

FIG. 1 is a block diagram illustrating the configuration of a fuel cell system 20 according to a preferred embodiment of the present invention.

FIG. 2 is a schematic cross-sectional view showing a configuration of a single cell 48 included in the fuel cell 40.

FIG. 3 is an explanatory diagram showing an outline of a configuration of a fuel reformer 22.

FIG. 4 is a flowchart illustrating a start-time processing routine executed when the fuel cell system 20 of the first embodiment is started.

FIG. 5 is a flowchart illustrating a temperature-raising processing routine executed after the fuel cell system 20 of the first embodiment is started.

FIG. 6 is an explanatory diagram showing a state in which the temperature of the reforming catalyst increases with time and a state in which the amount of generated hydrogen increases when the fuel reforming apparatus is started.

FIG. 7 is an explanatory diagram schematically showing the configuration of a fuel reforming apparatus 22a according to a second embodiment.

FIG. 8 is a flowchart illustrating a temperature-raising processing routine executed after the fuel cell system according to the second embodiment is started.

FIG. 9 is an explanatory view schematically showing a configuration of a fuel reforming apparatus 22b according to a third embodiment.

FIG. 10 is a flowchart illustrating a temperature-raising processing routine executed after the fuel cell system according to the third embodiment is started.

FIG. 11 is an explanatory view schematically showing a configuration of a fuel reforming apparatus 22c according to a fourth embodiment.

FIG. 12 is an explanatory diagram schematically illustrating the configuration of a fuel cell system 20d.

[Explanation of symbols]

 20, 20d ... fuel cell system 22, 22a, 22b, 22c ... fuel reformer 24 ... condensed water recovery unit 26 ... CO reduction unit 28 ... methanol tank 30 ... water tank 32 ... compressor 32a ... turbine 32b ... compressor 32c ... Shaft 33 ... Exhaust gas recovery path 34, 34a, 34b, 34c ... Burner 35 ... Water recovery path 36 ... Air tank 37 ... Valve 38 ... Compressor 40 ... Fuel cell 41 ... Electrolyte membrane 42 ... Anode 43 ... Cathode 44, 45 ... Separator 44P ... Fuel gas channel 45P Oxidizing gas channel 46, 47 Current collector 48 Single cell 50 Controller 52 Input / output port 54 CPU 56 ROM 58 RAM 60 First temperature sensor 61 Second temperature Sensor 62: Third temperature sensor 63: Fourth temperature sensor 64: First pump 65: Second port Step 66: Third pump 67 ... Pressure sensor 68 ... First flow rate regulator 69 ... Air introduction path 70 ... Methanol flow path 71 ... Methanol branch path 72 ... Water supply path 73 ... Oxidation exhaust gas path 74 ... Fuel exhaust gas path 76 ... First Air supply path 77 ... second air supply path 78 ... first fuel supply path 79 ... second fuel supply path 80 ... third fuel supply path 81 ... fuel branch path 82 ... third air supply path 83 ... second flow rate regulator 84 third flow regulator 87 switching valve 88 fuel gas passage 89 electromagnetically operated valve 89c thermally operated valve 90, 90a, 90b, 90c evaporation section 91, 91c pressure release valve 92, 92a, 92b, 92c ... reforming section 93 ... air supply branching passages 94, 94a, 94b, 94c ... combustion exhaust gas introduction section 95 ... combustion exhaust gas pipe 96 ... heat pipe 97 ... fourth flow rate regulator 98 ... fin

Claims (8)

[Claims] 1. A fuel reformer that uses a hydrocarbon as a raw fuel, vaporizes at least a liquid containing the raw fuel, generates a raw fuel gas, and performs a reforming reaction to generate a fuel gas containing hydrogen from the raw fuel gas. A heat generation unit that generates a high-temperature gas capable of supplying heat required for vaporizing the liquid containing the raw fuel, the heat generation unit including the high-temperature gas generated by the heat generation unit and the raw fuel A liquid is supplied, and by performing heat exchange between the liquid and the high-temperature gas, the raw fuel gas is generated from the liquid and, at the same time, evaporating to discharge exhaust gas generated after the high-temperature gas exchanges heat. Unit, a supply raw fuel amount control means for adjusting the amount of the liquid supplied to the evaporating unit, a predetermined reforming catalyst, receiving the supply of the raw fuel gas heated in the evaporating unit, The raw fuel gas is A reforming unit that causes the reforming reaction to proceed by passing through a surface of a catalyst; a calorie moving unit that moves a calorie included in the exhaust gas to the reforming unit; By limiting the amount of the liquid supplied to the raw material via the raw fuel amount control means, the amount of heat exchanged from the high-temperature gas to the liquid in the evaporator is reduced, and the exhaust gas temperature is reduced to a predetermined value. A fuel reformer comprising: a controller configured to perform an exhaust gas temperature raising control for raising the temperature to a high temperature and, when the fuel reformer is in a steady state, perform a control of the exhaust gas temperature raising control with respect to an amount of the liquid supplied to the evaporator. Quality equipment. 2. The fuel reforming apparatus according to claim 1, wherein the fuel reforming apparatus is in a steady state and the exhaust gas temperature raising control relating to an amount of the liquid supplied to the evaporator is not performed. Controlling the temperature of the high-temperature gas generated in the calorific value generating unit based on information on the amount of the liquid supplied to the evaporating unit, and setting the temperature of the exhaust gas discharged from the evaporating unit to a predetermined temperature. A fuel reforming apparatus comprising: a high-temperature gas temperature control unit configured as described below; and a heating unit configured to supply a heat amount required for the reforming reaction to the reforming unit when the fuel reforming unit enters a steady state. 3. The heat transfer means is provided inside the reforming section, and is formed so as to be capable of selectively transporting heat from an exhaust gas discharged from the evaporation section toward the inside of the reforming section. 3. The fuel reformer according to claim 1, wherein the fuel reformer comprises a heat pipe. 4. The fuel reforming apparatus according to claim 1, wherein the calorie transfer means is capable of introducing the exhaust gas, and heat is transferred between the introduced exhaust gas and the reforming section. A first exhaust gas passage where exchange is performed, a second exhaust gas passage capable of introducing the exhaust gas, and discharging the exhaust gas to the outside without exchanging heat with the reforming unit; When the fuel reforming apparatus is started, the flow path of the exhaust gas is the first exhaust gas flow path, and the exhaust gas temperature control is not performed with respect to the amount of the liquid to be supplied to the evaporating section. And a flow path switching means for switching the flow path to the second exhaust gas flow path. 5. The heating means for supplying heat required for the reforming reaction when the fuel reforming device is in a steady state is a heater provided in the reforming section. Fuel reformer. 6. The heating means for supplying heat required for the reforming reaction when the fuel reforming device is in a steady state includes a heat generated by an oxidation reforming reaction which proceeds inside the reforming section. 3. The fuel reformer according to claim 2, wherein the fuel reformer is a unit that utilizes a fuel. 7. The fuel according to claim 1, wherein the raw fuel is methanol.
7. The fuel reformer according to any one of claims 6 to 6. 8. The fuel reformer according to claim 1, wherein the liquid containing the raw fuel is a mixture of the raw fuel and water in a liquid state or the raw fuel in a gas state. A fuel reformer that is a mixture with water, and wherein the reforming reaction that proceeds in the reforming section includes at least a steam reforming reaction.