JP2002276909A - Burner - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a burner excellent in combustion performance. SOLUTION: A plurality of nozzle pipes N for combustion are juxtaposed and an injection direction of gas through a burner port (a) of each of the nozzle pipes N is set such that injection gas through the burner ports (a) of the nozzle pipes N collide with each other.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for producing combustion heat for reforming raw fuel in a reformer for a fuel cell by burning exhaust gas discharged from a fuel cell, for example. The present invention relates to a premix burner used in various industrial fields such as a burner.

[0002]

2. Description of the Related Art In a conventional burner of this type, combustion air or fuel gas is jetted from a central jet port, and fuel gas or combustion air is jetted from a peripheral jet port as a swirling flow to mix the two. It was made to burn.

[0003]

However, in the case of the above-mentioned conventional technique, although the mixing property of both gases can be improved as compared with the case where the swirling flow is not used because the gas is ejected as a swirling flow, it is substantially possible. Is only in contact with both gases, so poor mixing, unburned components in exhaust gas, etc.
There was room for improvement in terms of combustion. Further, in a flat combustion space as shown in the embodiment, there is also a problem that it is difficult to realize a swirling flow due to its structure.

[0004] An object of the present invention is to provide a burner excellent in flammability.

[0005]

The features, operations and effects of the burner according to the present invention according to claim 1 are as follows.

[Characteristics] A plurality of combustion nozzle tubes are arranged in parallel, and the direction of gas ejection from the flame holes of each nozzle tube is set so that the gas ejected from the flame holes of each nozzle tube collides with each other. At one point.

[Action] Since the jet gas from the flame hole of each nozzle tube collides with each other by effectively utilizing the fact that a plurality of nozzle tubes are juxtaposed, the jet gas is satisfactorily mixed by the collision. be able to.

[Effects] Therefore, the flammability can be improved by a simple structure improvement such as devising and arranging the flame holes.

The features, functions and effects of the burner according to the second aspect of the present invention are as follows.

[Features] In the burner according to the present invention according to the first aspect, fuel gas is supplied to at least one of the nozzle tubes, and combustion air is supplied to the other nozzle tubes. It is in.

[Function] Since the fuel gas ejected from one nozzle tube and the combustion air ejected from another nozzle tube collide with each other so that the two can be mixed well, good combustion properties can be obtained. Can be.

[Effect] Accordingly, it is possible to provide a burner useful as a burner for premixing and burning fuel gas and combustion air. Further, even if the fuel gas is a gas having a high burning rate such as hydrogen, the flashback can be completely prevented because the fuel gas is premixed.

The features, functions and effects of the burner according to the third aspect of the present invention are as follows.

[Features] In the burner according to the first aspect of the present invention, a gas mixture of fuel gas and combustion air is supplied to each of the nozzle tubes.

[Operation] Since the mixed gas ejected from each nozzle pipe is caused to collide with each other so that the mixed gas can be satisfactorily mixed, the flammability can be improved.

[Effect] Accordingly, a burner useful as a burner for burning a mixed gas can be provided.

The features, operations and effects of the burner according to the present invention according to claim 4 are as follows.

[Features] In the burner according to the first aspect of the present invention, a mixed gas of fuel gas and combustion air is supplied to at least one of the nozzle tubes, and discharged from the fuel cell to another nozzle tube. That is, it is configured so as to supply exhausted fuel gas.

[Function] Since the mixed gas ejected from a certain nozzle tube and the exhaust fuel gas ejected from another nozzle tube collide with each other so that the two can be mixed well, good combustibility can be obtained. Can be.

[Effect] Accordingly, it is possible to provide a burner useful as a burner for a fuel cell for burning exhaust fuel gas.

The features, operations and effects of the burner according to the present invention according to claim 5 are as follows.

[Features] In the burner according to the first aspect of the present invention, the burner is for generating combustion heat for reforming raw fuel in a reformer for a fuel cell.

[Operation] Since the combustibility is good, combustion heat can be efficiently generated with a small amount of fuel.

[Effect] Accordingly, a burner useful as a burner for generating combustion heat for reforming treatment in a reformer for a fuel cell can be provided.

[0025]

Embodiments of the present invention will be described below with reference to the drawings. In the following embodiment, a hydrogen-containing gas generator P including a reformer A according to the present invention will be described. However, the reformer A includes a reformer R for reforming raw fuel and a reformer R. The hydrogen-containing gas generator P is configured to include a steam generator S that generates steam for processing, and the hydrogen-containing gas generator P is included in the reforming process gas reformed in the reformer R in addition to the reformer A. A conversion treatment unit 5 and a selective oxidation treatment unit 6 for reducing the amount of carbon monoxide gas to be produced, so as to generate a hydrogen-rich fuel gas having a low carbon monoxide gas concentration (for example, 10 ppm or less). I have.

As shown in FIG. 1, a hydrogen-containing gas generator P includes a desulfurization processing section 1 for desulfurizing a hydrocarbon-based raw fuel gas such as natural gas, and a steam generation section for generating steam for reforming. The raw fuel gas desulfurized in the desulfurization processing section 1 is converted into hydrogen gas and carbon monoxide using the steam generated in the steam generation section S by the combustion heat of the section S and the exhaust fuel gas discharged from the fuel cell G. A reforming section R for reforming the gas, a reforming section 5 for transforming carbon monoxide gas in the reforming gas discharged from the reforming section R into carbon dioxide gas using steam, A selective oxidation treatment section 6 for selectively oxidizing carbon monoxide gas remaining in the shift gas discharged from the shift processing section 5 is provided.

Although a detailed description of the fuel cell G is omitted,
It is a solid polymer type using a polymer membrane as an electrolyte, and is supplied from the hydrogen-containing gas generator P through the fuel gas passage 23 through the fuel gas passage 23 and from the reaction blower 14 through the reaction air passage 32. It is configured to generate power by an electrochemical reaction with oxygen in the reaction air.

The reforming section R is filled with a reforming catalyst in a gas-permeable manner, and the gas to be reformed (mixed gas of desulfurized raw fuel gas and water vapor) is passed therethrough to reform the raw fuel gas. And a combustion unit 4 that burns the exhaust gas discharged from the fuel cell G and heats the reforming unit 3.

The steam generation section S includes a steam generation heating flow section 11 through which the combustion gas discharged from the combustion section 4 of the reforming section R flows, and a steam flow generation heating flow section through which the supplied raw water is supplied. And an evaporating unit 2 for evaporating by heating by the heating unit 11.

Further, a high-temperature reforming gas discharged from the reforming section 3 is passed through the hydrogen-containing gas generator P, and a heat-retaining flow section 7 for keeping the reforming section 3 warm is provided. And a heat exchanger Ep for the gas to be reformed, which heats the gas to be reformed supplied to the reforming section 3 with the high-temperature reforming gas, and is supplied to the desulfurization section 1 with the gas to be reformed at high temperature. A raw fuel gas heat exchanger Ea for heating the raw fuel gas, a metamorphic section cooling passage 8 for passing a cooling fluid to cool the metamorphic processing section 5, and a cooling section for cooling the metamorphic processing section 6 as well. And a cooling fan 10 for cooling the metamorphic treatment unit 5 and the selective oxidation treatment unit 6.
Are provided. Further, the heat exchanger 1 for preheating a raw water for preheating the raw water by exchanging heat between the metamorphic processing gas discharged from the metamorphic processing section 5 and the raw water supplied to the steam generating section S.
7 is provided.

The heat exchanger Ep for the gas to be reformed includes an upstream reforming gas flow section 12 through which the reforming gas discharged from the heat retaining flow section 7 flows, and a reforming section 3. A heat exchange unit for raw fuel gas Ea is provided so as to exchange heat with the gas to be reformed 13 through which the gas to be supplied flows. The downstream reforming gas flow section 15 through which the discharged reforming gas flows and the raw fuel gas flowing section 16 through which the raw fuel gas supplied to the desulfurization processing section 1 flows can exchange heat freely. It is provided and configured.

In the present invention, the combustion section 4 has a flaming combustion section 4F for burning the exhaust fuel gas in a state of forming a flame.
And the flaming combustion section 4F
And a catalyst combustion unit 4C that is disposed on the lower side in the flame formation direction and that causes the combustion catalyst 4c to burn the exhaust fuel gas not burned in the flaming combustion unit 4F.

As shown in FIG. 2, the hydrogen-containing gas generating apparatus P is provided with a plurality of flat plates B having a rectangular plate shape arranged in the thickness direction of the plate shape. Section, each flow section, the combustion section 4, and the like.

A part of the plurality of containers B is constituted by a single-chamber-equipped container Bm formed to have one chamber, and the rest is a twin-chamber formed to have two partitioned chambers. It is composed of a storage container Bd.

As shown in FIGS. 2 to 5, the double-chambered container Bd basically includes a flat partition member 43 between a pair of dish-shaped container forming members 41 and a peripheral portion thereof. The sections are welded together to define two flat chambers. The reforming unit R is configured using one twin-chambered container Bd, and the steam generating unit S is also configured using one double-chambered container Bd. Among the twin chamber-equipped container Bd, the twin chamber-equipped container Bd constituting the reforming section R is, as shown in FIGS. 2 to 4, a flat-bottomed dish-shaped container forming member 41 having a flat bottom.
In a state where the flat partition member 43 is located between the two-stage dish-shaped container forming member 41 in which one side of the bottom is deepened, the peripheral portion is welded and connected to partition the two chambers. It is formed. Further, in the twin chamber-equipped container Bd, the steam generator S
As shown in FIG. 2, the twin chamber-equipped container Bd is formed between a flat-bottomed dish-shaped container forming member 41 and a convex dish-shaped container forming member 41 having a raised bottom. With the plate-like partition member 43 positioned, the peripheral portions are welded and connected to define two chambers. Twin room equipped container Bd
Of the components other than those constituting the reforming section R and the steam generating section S, as shown in FIG. 5, a flat partition member 43 is positioned between a pair of flat bottom dish-shaped container forming members 41. In this state, two flat chambers are formed by welding and connecting the peripheral portions.

As shown in FIG. 6, the single-chambered container Bm
The periphery of the dish-shaped container forming member 41 and the flat-plate-shaped container forming member 42 are connected by welding to define one flat chamber. A connection nozzle 44 for fluid supply or fluid discharge is attached to each of the single-chamber-equipped containers Bm and each of the double-chamber-equipped containers Bd so as to communicate with the internal chambers as necessary.
Although not shown, if necessary, the chamber of the container B is configured to have a meandering flow path, and the flow path of the fluid is lengthened.

As shown in FIGS. 2 to 4, the double-chambered container Bd constituting the reforming section R is adjusted so that the deep part of the two-stage dish-shaped container forming member 41 is located on the lower side. And a two-stage dish-shaped container forming member 41 and a partition member 43
Combustion unit 4 using a portion having a flat chamber formed by
The reforming processing unit 3 is configured using a portion having a flat chamber formed by a flat bottom dish-shaped container forming member 41 and a partition member 43.

A flat chamber having a large depth on the lower side formed by the two-stage dish-shaped container forming member 41 and the partition member 43 is defined as a combustion chamber 4r, and the combustion gas is supplied to the lower end of the combustion chamber 4r. An elongated burner 4b is arranged along the lower edge so as to jet into the combustion chamber 4r over substantially the entire width thereof to form a flaming combustion section 4F, and the depth above the combustion chamber 4r is narrow. A combustion catalyst 4c is arranged in the portion to constitute a catalyst combustion section 4C. 4i in the figure is an igniter for igniting the burner 4b.

That is, the combustion chamber 4r has a large area of each of a pair of wall portions facing each other side by side in a direction orthogonal to the flame forming direction of the flaming combustion portion 4F (ie, the direction of flowing the combustion gas). The space between the pair of wall portions is formed in a narrow flat shape, the flat combustion chamber 4r is vertically arranged, and the flaming combustion portion 4F is formed below the combustion chamber 4r in the flame forming direction. The catalytic combustion unit 4C is disposed so as to face upward, and is disposed above the flaming combustion unit 4F in the combustion chamber 4r, that is, at a position below the flaming combustion unit 4F in the flame formation direction. is there. The combustion catalyst 4c is made of platinum, palladium or the like.

The burner 4b is, as shown in FIGS.
Two nozzle pipes N are juxtaposed horizontally in a state of being close to each other,
The gas ejection direction from the flame hole a of each nozzle tube N is set such that the gas ejected from the flame hole a of each nozzle tube N collides with each other. Specifically, the flame hole a is formed so as to eject gas obliquely upward in a direction facing each other, and the angle θ formed with the horizontal plane in the ejection direction is 0.
To 45 degrees, preferably about 30 to 45 degrees. The exhaust fuel gas is supplied to one nozzle pipe N via the exhaust fuel gas path 24, and the combustion air path 2 is supplied to the other nozzle pipe N.
Combustion air is supplied via the nozzle 9, and the exhaust fuel gas ejected from the flame hole a and the combustion air collide with each other and are supplied to the flaming combustion section 4 </ b> F.

The flat chamber constituting the reforming section 3 is filled with a large number of porous ceramic particles holding a reforming catalyst such as ruthenium, nickel, platinum or the like in a gas-permeable state. .

As shown in FIG. 2, a double-chambered container Bd constituting the steam generating section S is erected, and is formed by a convex dish-shaped container forming member 41 and a flat partition member 4. The portion having the chamber is used to constitute the evaporation chamber 2, and the portion having the flat chamber formed by the flat bottom dish-shaped container forming member 41 and the partition member 43 is used to heat the steam generation. The flow section 11 is formed, and both chambers are filled with a heat transfer promoting material made of stainless steel wool or the like in a permeable state.

As shown in FIG. 2, in this embodiment, eight double-chambered containers Bd and one single-chambered container B
m is the third single-chamber container B from the left end in side view.
In a state where m is located, the unit is provided side by side in the thickness direction to form a compact. Eight twin chamber equipped containers B
For the sake of clarity, for the sake of simplicity, the code 1, which indicates the arrangement order from the left, after the code Bd indicating the double-chamber-equipped container, for convenience.
2, 3 ... 8

The steam generating section S is constituted by the double chamber-equipped container Bd1 on the left end, and the reforming section R is constituted by the second twin chamber-equipped vessel Bd2 from the left. Using the single chamber equipped container Bm,
A heat retaining flow section 7 is formed.

The upstream reforming gas flow section 12 is constituted by using the left chamber of the third double-chamber container Bd3 from the left, and the section having the right chamber is formed by using the right chamber. , A gas passage section 13 for the reformed gas. Both chambers are filled with a heat transfer promoting material made of stainless steel wool or the like in a permeable state.

The desulfurization treatment section 1 is constituted by using the portion provided with the left chamber of the fourth double-chamber container Bd4 from the left, and the flow of the raw fuel gas is carried out using the portion provided with the right chamber. The unit 16 is constituted. A large number of ceramic porous granules holding a desulfurization catalyst are filled in the left chamber constituting the desulfurization unit 1 in a gas-permeable state.

The portion of the fifth double chamber-equipped container Bd5 from the left with the left chamber is used to constitute the downstream reforming gas flow section 15 and the portion with the right chamber is used. , A metamorphic processing unit 5. Sixth double-chamber container B from the left
The metamorphic treatment section 5 is constituted by using the portion provided with the left chamber of d6, and the metamorphic section cooling passage 8 is constituted by using the portion provided with the right chamber. The metamorphic treatment unit 5 is configured by using the seventh double-chambered container Bd7 from the left. Each of the chambers constituting the shift processing section is filled with a large number of porous ceramic particles holding a shift reaction catalyst of iron oxide or copper zinc in a gas-permeable state.

The eighth (right end) double-chambered container Bd from the left
The portion provided with the left chamber of FIG. 8 constitutes the flow passage 9 for cooling the metamorphic section, and the portion provided with the right chamber constitutes the selective oxidation treatment section 6. The interior of the chamber constituting the selective oxidation treatment section 6 is filled with a large number of porous ceramic particles holding a ruthenium selective oxidation catalyst in a gas-permeable state.

In arranging a plurality of containers B including eight double-chambered containers Bd and one single-chambered container Bm, those which need to be heat-transferred are in close contact with each other, and They are arranged in a state in which a heat insulating material 19 for adjusting the amount of heat transfer is interposed between members that need to adjust the amount of heat. That is, the heat insulating material 19 is arranged between the leftmost double-compartment container Bd1 constituting the steam generating section S and the second twin-compartment container Bd2 from the left constituting the reforming section R,
The second twin-compartment container Bd2 and the single-compartment container Bm are closely arranged, and the heat insulating material 19 is arranged between the single-compartment container Bm and the third double-compartment container Bd3 from the left. Third twin-chamber container Bd3 and fourth twin-chamber container Bd from the left
4, and the fourth to eighth (right end) twin chamber-equipped containers Bd4 to Bd8 from the left are closely arranged to each other.

That is, in a state where a plurality of containers B are juxtaposed, the twin chamber-equipped container Bd2 constituting the reforming section R, which is required to maintain the highest temperature, is arranged at a substantially intermediate portion in the juxtaposition direction. The heat insulating material 19 is arranged on one side of the double chamber-equipped container Bd2 constituting the quality part R, and the single chamber-equipped container Bm and the heat insulator 19 constituting the heat retaining flow part 7 are arranged on the other side. On each side, so that the processing temperature is in the order of decreasing generally,
The hydrogen-containing gas generator is provided by arranging the containers B constituting the respective processing sections and the like, and arranging the twin chamber-equipped vessel Bd8 constituting the selective oxidation processing section 6 requiring cooling at the end in the juxtaposition direction. The heat dissipation loss can be suppressed as much as possible while the P is made compact, and each processing section can be controlled to an appropriate temperature.

The reformer A having the reforming section R and the steam generating section S will be described in more detail. One side of the flat combustion section 4 of the reforming section R is provided with a flat reforming section 3. Are arranged side by side in the thickness direction and closely arranged via a flat partition member 43 functioning as a heat transfer wall, and a flat-shaped steam generation section is provided on the other side of the combustion section 4 via a heat insulating material 19. S are arranged side by side in the thickness direction, and the reformer A
Is compactly constructed. In addition, by adopting such an arrangement, heat dissipation from the combustion section 4 is suppressed, and the flat combustion section 4 and the reforming section 3 each function as a heat transfer wall. Through
By closely disposing in the thickness direction, the heat transfer area is widened, the heat dissipation from the combustion part 4 is suppressed, and the heating efficiency is effectively improved by the synergistic effect of heating in the wide heat transfer area. I have.

Further, the flat-shaped heating flow passage 11 for steam generation and the evaporation processing chamber 2 are closely arranged in the thickness direction via a flat partition member 43 functioning as a heat transfer wall. The heat transfer area is widened, and the heating efficiency is effectively improved.

In the reforming section 3, when natural gas mainly composed of methane gas is a raw fuel gas, methane gas and water vapor are converted by the following reaction formula under heating at, for example, about 700 to 750 ° C. Through a reforming reaction, the gas is reformed into a gas containing hydrogen gas and carbon monoxide gas.

[0054]

Embedded image CH ₄ + H ₂ O → CO + 3H ₂

In the metamorphic treatment section 5, the carbon monoxide gas in the reforming gas and the water vapor undergo a metamorphic reaction at a reaction temperature of, for example, about 200 ° C. according to the following reaction formula. Is converted into carbon dioxide gas.

[0056]

## STR2 ## CO + H ₂ O → CO ₂ + H ₂

In the selective oxidation treatment section 6, the reaction temperature is about 100 ° C. by the catalytic action of ruthenium.
The carbon monoxide gas remaining in the shift gas is selectively oxidized.

In FIGS. 1 and 2, the raw fuel gas supply passage 21 is connected to the raw fuel gas passage 16 of the raw fuel gas heat exchanger Ea as indicated by the white arrow, and Fuel gas flow section 16, desulfurization processing section 1, reformed gas flow section 13 of reformed gas heat exchanger Ep, reforming processing section 3, warming flow section 7, heat for reformed gas The gas flowing in the order of the upstream reforming gas flow section 12 of the exchanger Ep, the downstream reforming gas flow section 15 of the raw fuel gas heat exchanger Ea, each shift processing section 5, and the selective oxidation processing section 6. They are connected by a gas processing channel 22 so as to form a processing path. A raw water preheating heat exchanger for preheating the raw water flowing through the raw water supply passage 25 with the metamorphic processing gas is provided in the gas processing flow path 22 connecting the last stage shift processing unit 5 and the selective oxidation processing unit 6. 17 and a drain trap 34 for removing condensed water from the shift gas is provided downstream of the raw water preheating heat exchanger 17 to exchange heat between the shift gas and the raw water. In addition, the raw water is preheated and the shift gas is cooled.

The temperature of the shift gas discharged from the shift processing section 5 is about 200 ° C. and the reaction temperature in the selective oxidation section 6 is about 100 ° C. In this method, the shift gas is cooled to a temperature near the reaction temperature in the selective oxidation section 6, and the heat recovered by the cooling is used for preheating the raw water.

Then, the raw fuel gas supplied from the raw fuel gas supply passage 21 is desulfurized in the desulfurization processing section 1, and the desulfurized raw fuel gas is mixed with steam from a steam passage 26, which will be described later, and reformed. The reforming gas is supplied to the processing unit 3, the reforming gas is sequentially supplied to the four-stage shift processing unit 5, the carbon monoxide gas is converted to carbon dioxide gas, and the shift processing gas is selected. The carbon monoxide gas is supplied to the oxidizing section 6 and selectively oxidized.

The selective oxidation processing gas discharged from the selective oxidation processing section 6 is supplied as fuel gas to the fuel cell G through the fuel gas passage 23, and the exhaust fuel gas discharged from the fuel cell G is discharged into the exhaust fuel gas passage 24. Is supplied to one nozzle pipe N of the reforming burner 4b. Note that the temperature of the selective oxidation processing gas discharged from the selective oxidation processing section 6 is about 110 ° C., and the operating temperature of the polymer fuel cell G is about 80 ° C. , Selective oxidation processing section 6
A fuel gas cooling heat exchanger 33 is provided for cooling the selective oxidizing gas discharged from the fuel cell to near the operating temperature of the fuel cell G.

1 and 2, a raw water supply passage 25 for supplying raw water for generating steam is connected to the evaporating chamber 2 of the steam generating section S, as indicated by solid arrows. Steam path 26 which sends out the steam generated in
Is connected to a gas processing flow path 22 that connects the desulfurization processing section 1 and the reformed gas flow section 13, and the desulfurization raw fuel gas flowing through the gas processing flow path 22 is subjected to reforming steam. Are configured to be mixed.

In the raw water supply passage 25, the raw water preheating heat exchanger 17 is provided. Further, the raw water is supplied to a part of the raw water supply passage 25 downstream of the raw water preheating heat exchanger 17. A meandering flow portion 18 that flows in a meandering shape is provided, and the meandering flow portion 18 is applied to a portion of the outer wall of the steam generator P that covers the combustion portion 4 of the reforming portion R in a heat conductive manner. The feed water flowing through the meandering flow portion 18 is preheated by conduction heat and radiant heat from the outer wall of the hydrogen-containing gas generator P. Then, the raw water to be supplied to the steam generating section S is preheated by the raw water preheating heat exchanger 17 and the meandering flow section 18.

1 and 2, the combustion gas discharged from the combustion section 4 of the reforming section R is passed through the heating flow section 11 for steam generation and the flow section for cooling the shift section, as indicated by the dashed arrows. 8, the combustion section 4, the steam-generating heating flow section 11, and the metamorphic section cooling flow section 8 are passed through the combustion gas passage 27.
In the heating flow section 11 for steam generation, the evaporative treatment chamber 2 is heated by the combustion gas, and in the flow section 8 for cooling the metamorphic section, a metamorphic reaction which is an exothermic reaction is caused by the combustion gas. It is configured to cool the metamorphic processing unit 5 to be performed. The temperature of the combustion gas discharged from the steam-generating heating passage 11 is about 120 ° C., and the combustion gas flows through the metamorphic section cooling passage 8 to cool the metamorphic processing section 5. Since the temperature of the combustion gas discharged from the cooling section cooling passage 8 has risen to about 150 ° C., an exhaust heat recovery heat exchanger (not shown) is provided to recover the exhaust heat from the combustion gas. Produces steam and hot water.

In FIGS. 1 and 2, as indicated by a dashed line arrow, the air from the combustion blower 28 is used as combustion air to flow through the flow passage 9 for cooling the shift section, and then the reforming section. The combustion blower 28 and the cooling section cooling passage 9 are connected by a combustion air passage 29 so that the combustion air is supplied to the other nozzle pipe N of the R reforming burner 4b. The combustion air passage 29 is connected to a combustion air bypass passage 30 so as to bypass the cooling flow passage 9 and flow therethrough, and the air from the combustion blower 28 is used as oxidation air to the selective oxidation treatment unit 6. The oxidizing air supply path 31 connected to the combustion blower 28 is connected to the gas processing flow path 22 that connects the metamorphic processing section 5 and the selective oxidation processing section 6 at the last stage so as to supply the gas.

A state in which combustion air is supplied to the other nozzle pipe N of the reformer burner 4b by flowing it through the flow passage 9 for cooling the metamorphic portion, and a condition where the combustion air is bypassed. On-off valves 35 and 36 are provided in order to switch to a state of supplying the fuel through the combustion air bypass 30. Normally, the on-off valves 35 and 36 are switched to a state in which the combustion air flows through the combustion air bypass 30. However, when the cooling capacity of the metamorphic treatment unit 5 is insufficient, for example, during a high temperature in summer, Then, the on-off valves 35 and 36 are switched to a state in which the combustion air flows through the metamorphic section cooling passage 9 to cool the metamorphic processing section 5 with the combustion air.

Next, the control configuration of the hydrogen-containing gas generator P will be described. As shown in FIG. 1, a raw fuel gas supply path 21 is provided with a raw fuel supply amount control valve 37 for adjusting the raw fuel gas supply amount. A temperature sensor 38 for detection is provided, and a control unit 39 for controlling the operation of each of the raw fuel supply amount control valve 37, the reaction blower 14, the combustion blower 28, and the igniter 4i is provided.

Hereinafter, the control operation of the control section 39 will be described.
When there is an operation start command from an operation unit (not shown), the control unit 39 activates the combustion blower 28 and supplies starting gas fuel such as 13A from a starting gas fuel supply path (not shown). The igniter 4i is supplied to one nozzle pipe N of the burner 4b in the combustion section 4 to operate the igniter 4i.
When the temperature detected by the temperature sensor 38 becomes equal to or higher than a target temperature set in advance to a predetermined temperature at which the reforming process can be performed, the raw fuel supply amount control valve 37 is opened, and the reforming process section is opened. In step 3, the reforming process of the raw fuel gas is started, and the reaction blower 14 is operated to start power generation of the fuel cell G.

The exhaust fuel gas is discharged from the fuel cell G,
When the raw fuel gas can be reformed by the heat of combustion of the exhaust fuel gas, the supply of the starting gas fuel from the starting gas fuel supply path is stopped, and the exhaust gas discharged from the fuel cell G is discharged. The entire amount of the fuel gas is received in one nozzle pipe N of the burner 4b and burned in the combustion unit 4, and the reforming unit 3 reforms the raw fuel gas by the combustion heat.

As an electric load on the fuel cell G, a current measuring device 4 for detecting an output current from the fuel cell G
Based on the detected value of 0, the raw fuel supply amount control valve 37 is controlled so that the raw fuel gas supply amount to the reforming section 3 becomes an amount corresponding to the electric load of the fuel cell G, and the fuel cell G The reaction blower 14 is controlled so that the amount of reaction air supplied to the fuel cell G becomes an amount corresponding to the electric load of the fuel cell G, and the detected temperature of the temperature sensor 38 becomes the target temperature.
By controlling the combustion blower 28, the supply amount of combustion air to the other nozzle tube N of the burner 4b, that is, the combustion section 4 is adjusted. That is, when the temperature detected by the temperature sensor 38 becomes higher than the target temperature, the combustion air supply amount is increased and adjusted so that the temperature detected by the temperature sensor 38 becomes the target temperature,
On the other hand, when the temperature detected by the temperature sensor 38 becomes lower than the target temperature, the supply amount of combustion air is reduced and adjusted so that the temperature detected by the temperature sensor 38 becomes the target temperature.

As described above, the combustion part 4 is divided into the flaming combustion part 4
F and the catalytic combustion unit 4C,
Since the rate of decrease of the electric load is large, the temperature detected by the temperature sensor 38 becomes higher than the target temperature, the rate of increase of the supply amount of combustion air increases, and the supply amount of combustion air becomes smaller than the amount of exhaust fuel gas received. Even if the flammable combustion section 4F blows out and misfires, the exhaust fuel gas is discharged from the combustion catalyst 4 which is heated to a reactive state.
Since combustion is performed by c, the stable combustion of the received exhaust fuel gas can be continued. Thereafter, the reforming temperature is lowered by adjusting the increase in the supply amount of combustion air, and the decrease in the supply amount of combustion air is adjusted. Flaming combustion part 4
F is ignited, and the exhaust fuel gas burns again in the flaming combustion section 4F.

Further, since the rate of increase of the electric load is large, the temperature detected by the temperature sensor 38 becomes lower than the target temperature.
The rate of decrease in the supply amount of combustion air increases, and the decrease amount of the supply amount of combustion air increases.
Even if F causes incomplete combustion, the unburned portion of the exhaust fuel gas is burned by the combustion catalyst 4c which is heated to a responsive state, so that the entire amount of the received exhaust fuel gas can be stably burned. . Thereafter, the reforming process temperature rises due to the decrease adjustment of the supply amount of combustion air, and the flammable combustion section 4F returns to the complete combustion state with the increase adjustment of the supply amount of combustion air. However, even if the supply amount of combustion air is reduced and adjusted so that the temperature detected by the temperature sensor 38 becomes the target temperature, the amount of combustion air required to burn the entire amount of the received exhaust fuel gas is less than the required amount. For example, an adjustment range of the supply amount of combustion air is set in advance according to, for example, an electric load or the like.

[Alternative Embodiment] In the above embodiment, the burner 4b of the reformer A is shown as a burner.
To supply the combustion air to the other nozzle pipes N. Also, as shown in FIG.
A configuration in which a mixed gas of a fuel gas and combustion air is supplied to each nozzle pipe N may be employed.

In the above embodiment, a burner provided with two nozzle pipes N is shown, but a burner provided with three or more nozzle pipes N may be used.

[Brief description of the drawings]

FIG. 1 is a system diagram of a hydrogen-containing gas generator including a reformer for a fuel cell according to an embodiment.

FIG. 2 is a longitudinal sectional side view of a hydrogen-containing gas generator including a reformer for a fuel cell according to an embodiment.

FIG. 3 is a perspective view of a reforming unit.

FIG. 4 is a vertical sectional front view of a combustion section of a reforming section.

FIG. 5 is a perspective view of a twin-chambered container constituting the hydrogen-containing gas generator.

FIG. 6 is a perspective view of a single-chamber-equipped container constituting the hydrogen-containing gas generator.

FIG. 7 is a perspective view of a burner.

FIG. 8 is a sectional view of a burner.

FIG. 9 is a sectional view of a burner according to another embodiment.

[Explanation of symbols]

 N Nozzle tube a Flame hole G Fuel cell A Reformer

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification FI FI Theme Court ゛ (Reference) H01M 8/06 H01M 8/06 G (72) Inventor Norihisa Shinya Hiranocho, Chuo-ku, Osaka-shi, Osaka F-term (reference) No. 1-2, Osaka Gas Co., Ltd. (reference) 3K017 AA01 AA05 AB01 AB07 AC03 AD01 AD03 AG07 CA03 CA05 CB01 CB09 CD04 CE05 3K019 AA01 AA05 BA01 BA04 BB04 BD01 CC07 5H027 AA06 BA01 BA09 BA16

Claims (5)

[Claims] 1. A plurality of nozzle tubes for combustion are arranged in parallel, and the direction of gas ejection from the flame holes of each nozzle tube is set so that the gas ejected from the flame holes of each nozzle tube collides with each other. Burner. 2. The burner according to claim 1, wherein fuel gas is supplied to at least one of the nozzle tubes, and combustion air is supplied to another nozzle tube. 3. A structure in which a mixed gas of fuel gas and combustion air is supplied to each of the nozzle tubes.
Burner described. 4. A structure in which a mixed gas of fuel gas and combustion air is supplied to at least one of the nozzle tubes, and the exhaust gas discharged from the fuel cell is supplied to another nozzle tube. The burner according to claim 1. 5. The burner according to claim 1, wherein the burner generates combustion heat for reforming raw fuel in a reformer for a fuel cell.