JP2007261871A - Hydrogen-containing gas producing apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a hydrogen-containing gas producing apparatus that can appropriately produce a hydrogen-containing gas having a predetermined composition. <P>SOLUTION: The apparatus is equipped with: a reforming section 3 which reforms a hydrocarbon source fuel with steam to produce a reformed gas with hydrogen gas as a main component; a combusting section 6 which combusts a combustion fuel by a reforming burner 17 to heat the reforming section 3 so as to treat reforming, wherein a combustion exhaust gas of the reforming burner 17 exhausted from the combustion section 6 is made to pass to control a temperature in other process sections 2, 4 than the reforming section 3; and a controlling means C configured to adjust quantity supplied of the combustion fuel to the reforming burner 17 so as to control the temperature of the reforming section 3 to an appropriate set temperature. The controlling means C adjusts quantity supplied of combustion air to the reforming burner 17 so as to control the oxygen concentration in the combustion exhaust gas of the burner 17 to 4 to 8%, and corrects quantity supplied of combustion air to the reforming burner 17 so as to control the temperature of other process sections 2, 4 to a set temperature. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

The present invention comprises a reforming section for reforming a supplied hydrocarbon-based raw fuel and steam to generate a reformed gas containing hydrogen gas as a main component,
A combustion unit that burns fuel for combustion in a reformer burner and heats the reforming unit so as to be reformed; and
The combustion exhaust gas of the reforming burner discharged from the combustion unit is configured to flow for temperature control of another processing unit different from the reforming unit,
The control means for controlling the operation relates to a hydrogen-containing gas generator configured to adjust the amount of combustion fuel supplied to the reforming burner so that the temperature of the reforming section becomes a set appropriate temperature.

Such a hydrogen-containing gas generating apparatus burns combustion fuel in a combustion section with a reformer burner, and heats the reforming section so that it can be reformed. Reforming reaction with water vapor to generate reformed gas containing hydrogen gas as the main component, and temperature of other processing parts different from the reforming part using the combustion exhaust gas from the reforming burner discharged from the combustion part As a result, the temperature of the other processing unit is controlled so that the predetermined processing related to the generation of the hydrogen-containing gas can be performed. The generated hydrogen-containing gas is used as, for example, a fuel gas for power generation reaction in a fuel cell.
Then, the supply amount of the combustion fuel to the reforming burner is adjusted by the control means so that the temperature of the reforming section becomes the set appropriate temperature.

  In such a hydrogen-containing gas generating apparatus, conventionally, when the exhaust fuel gas discharged from the fuel cell is used as the combustion fuel of the reformer burner, the air ratio is 1.27 to 1.45 (in the combustion exhaust gas). The amount of combustion air supplied to the reforming burner was adjusted so that the oxygen concentration was approximately 4.7 to 7% (see, for example, Patent Document 1).

That is, by supplying combustion air so that the air ratio becomes 1.27 to 1.45, the supply amount of combustion air is increased and the amount of combustion exhaust gas of the reforming burner is increased.
Then, by increasing the amount of combustion exhaust gas of the reforming burner, the ratio of the amount of heat transferred from the combustion exhaust gas to the reforming unit and other processing units with respect to the amount of heat retained by the combustion exhaust gas (hereinafter referred to as the heat transfer ratio) To reduce the amount of heat transfer to the reforming part due to the flow of combustion exhaust gas, heat the reforming part to a temperature suitable for the reforming process, and treat the other processing part The temperature was adjusted to an appropriate temperature.

  Incidentally, in the above-mentioned Patent Document 1, as the other processing unit, a steam generation unit that generates water vapor that is supplied to the reforming unit by heating the supplied water, and a reforming process gas generated in the reforming unit A conversion section that converts carbon monoxide into carbon dioxide, and adjusts the temperature of the combustion exhaust gas discharged from the combustion section so that the steam generation section can generate steam, and after the temperature control of the steam generation section, It is constituted so that a part may be flowed so that temperature may be controlled so that modification processing is possible.

JP 2005-219991 A

  However, in the conventional hydrogen-containing gas generation device, the supply amount of combustion air to the reforming burner is adjusted so that the air ratio is 1.27 to 1.45, and the supply amount of combustion air is thus reduced. By passing the flue gas of the reforming burner that burns in a controlled state for temperature control of the other processing unit, the temperature of the other processing unit is adjusted accordingly, so the temperature of the other processing unit fluctuates. There was a problem that it was easy.

Incidentally, raw fuel may be used as combustion fuel for the reformer burner without using the exhaust fuel gas from the fuel cell. When comparing the case where the exhaust fuel gas is burned with the reformer burner and the case where the raw fuel is burned, the exhaust fuel gas contains carbon dioxide gas, water vapor, etc., so the air ratio is the same. If so, the amount of combustion exhaust gas is reduced when the raw fuel is burned.
Therefore, when raw fuel is used as the combustion fuel for the reforming burner, the amount of combustion exhaust gas from the reforming burner tends to decrease, so the heat transfer ratio from the combustion exhaust gas in the reforming section increases. The amount of heat transfer accompanying the flow of the combustion exhaust gas tends to increase, and the amount of heat transfer to the other processing unit decreases, so that the temperature of the other processing unit is more likely to fluctuate.

When the temperature in the other processing unit varies, the variation in processing related to the generation of the hydrogen-containing gas in the other processing unit increases, and accordingly, the hydrogen-containing gas cannot be generated appropriately.
For example, when the steam generation unit and the shift unit are provided as other processing units as described above, when the temperature of the steam generation unit varies, the amount of steam generated in the steam generation unit varies, and the raw fuel in the reforming unit The variation in the processing state of the reforming process increases, and when the temperature of the shift section varies, the variation in the processing state of the shift process in the shift section increases, and the oxidized gas in the reformed process gas after the shift process A hydrogen-containing gas cannot be generated so as to have a predetermined composition such as an increase in carbon concentration.

  This invention is made | formed in view of this situation, The objective is to provide the hydrogen containing gas production | generation apparatus which can perform the production | generation of hydrogen containing gas appropriately so that it may become a predetermined composition.

The hydrogen-containing gas generating apparatus of the present invention includes a reforming unit that generates a reforming treatment gas mainly composed of hydrogen gas by reforming a supplied hydrocarbon-based raw fuel and steam.
A combustion unit that burns fuel for combustion in a reformer burner and heats the reforming unit so as to be reformed; and
The combustion exhaust gas of the reforming burner discharged from the combustion unit is configured to flow for temperature control of another processing unit different from the reforming unit,
The control means for controlling the operation is configured to adjust the supply amount of the combustion fuel to the reforming burner so that the temperature of the reforming section becomes a set appropriate temperature,
In the first characteristic configuration, the control means adjusts the amount of combustion air supplied to the reforming burner so that the oxygen concentration in the combustion exhaust gas of the reforming burner is 4 to 8%, and A feature is that the supply amount of combustion air to the reforming burner is corrected so that the temperature of the other processing unit becomes a set temperature.

  That is, the air for combustion to the reforming burner is adjusted by the control means so that the oxygen concentration in the combustion exhaust gas of the reforming burner becomes 4 to 8% (corresponding to an air ratio of approximately 1.2 to 1.6). The supply amount of combustion air to the reforming burner is corrected so that the supply amount is adjusted and the temperature of the other processing unit becomes the set temperature.

  That is, by increasing the supply amount of combustion air so that the oxygen concentration in the combustion exhaust gas becomes 4-8% and increasing the amount of combustion exhaust gas of the reformer burner, This reduces the heat transfer ratio of the combustion exhaust gas and reduces the amount of heat transfer associated with the flow of combustion exhaust gas, so that the reforming section is heated to a temperature suitable for the reforming process and the other processing section is used in the other processing section. The temperature can be adjusted to an appropriate temperature for the treatment.

Then, the amount of the combustion exhaust gas is increased so that the temperature of the other processing unit can be adjusted to a temperature suitable for processing in the other processing unit, while the temperature of the other processing unit is adjusted to the set temperature. Since the supply amount of the combustion air to the quality burner is corrected, it is possible to suppress fluctuations in the temperature of the other processing units, and thus it is possible to suppress variations in processing in the other processing units.
For example, when the temperature of the other processing unit is lower than the set temperature, if the amount of combustion exhaust gas is increased by correcting the supply amount of combustion air to the reforming burner, Since the amount of heat transfer to each of the sections increases, the temperature of the other processing section can be raised.
On the other hand, if the temperature of the other processing unit is higher than the set temperature, the amount of combustion exhaust gas supplied to the reforming burner is corrected to decrease, and the amount of combustion exhaust gas is reduced. Since the amount of heat transfer to each of the sections is reduced, the temperature of the other processing section can be lowered.
Therefore, it has become possible to provide a hydrogen-containing gas generating apparatus that can appropriately generate a hydrogen-containing gas so as to have a predetermined composition.

In addition to the first feature configuration, the second feature configuration is
As the other processing unit, a water vapor generating unit for heating supplied water to generate water vapor to be supplied to the reforming unit, and carbon monoxide in the reforming treatment gas generated in the reforming unit And a metamorphic part that transforms to carbon,
The flue gas discharged from the combustion section is temperature-controlled so that the steam generation section can generate steam, and after the temperature control of the steam generation section, the conversion section is controlled to be temperature-controllable. Configured to flow,
Combustion air to the reforming burner so that the temperature of the steam generation unit becomes a set temperature for steam generation or the temperature of the shift unit becomes a set temperature for conversion. It is characterized in that it is configured to correct the supply amount.

That is, the flue gas discharged from the combustion section is tempered so that the steam generation section can generate steam, and after the temperature of the steam generation section is adjusted, the transformation section is tempered so that it can be transformed. In the steam generation unit, the supplied water is heated to generate steam, and the generated steam is supplied to the reforming unit for the reforming process, and in the shift processing unit, the steam is generated in the reforming unit. The carbon monoxide in the reformed gas is converted to carbon dioxide.
When the supply amount of combustion air to the reforming burner is corrected by the control means so that the temperature of the steam generating unit becomes the set temperature for generating steam, fluctuations in the temperature of the steam generating unit are suppressed. As a result, the steam generation in the steam generating section is stabilized and the amount of steam generated is stabilized, so that the reforming process of the raw fuel is performed more stably in the reforming section, and the reforming process gas The composition can be further stabilized.
Also, if the control means corrects the supply amount of combustion air to the reforming burner so that the temperature of the shift section becomes the set temperature for shift, fluctuations in the temperature of the shift section are suppressed. In the shift section, carbon monoxide in the reforming process gas can be further stably converted to carbon dioxide, and the composition of the reforming process gas after the shift process can be stabilized.
Therefore, the composition of the produced hydrogen-containing gas can be further stabilized.

The third feature configuration is in addition to the second feature configuration,
The steam generation unit is provided on one side of the reforming unit and the combustion unit in a state where heat can be transferred from the reforming unit and the combustion unit,
The transformation section is provided on the other side of the reforming section and the combustion section in a state where heat can be transferred from the reforming section and the combustion section.

  That is, heat is transferred from the reforming unit and the combustion unit to the steam generation unit provided on one side of the reforming unit and the combustion unit, and the reforming unit provided on the other side of the reforming unit and combustion unit is reformed. Heat is transferred from the part and the combustion part.

That is, the temperature at which water is generated in the steam generation unit by generating water and the temperature at which the carbon monoxide in the reformed gas is converted to carbon dioxide in the shift unit are both raw fuel in the reforming unit. The heat generation from the reforming section and the combustion section is made possible by distributing the steam generation section and the transformation section in a state where heat can be transferred to both sides of the reforming section and the combustion section. While suppressing loss and saving energy, it is possible to further suppress temperature fluctuations in the water vapor generation unit and the transformation unit.
Therefore, the composition of the produced hydrogen-containing gas can be further stabilized while saving energy.

In addition to any of the first to third feature configurations described above, the fourth feature configuration is
Other combustion equipment in which the reformed gas generated in the reforming unit is supplied to the fuel cell as a fuel gas for power generation, and the exhaust fuel gas discharged from the fuel cell is different from the reforming burner Configured to burn at
A feature is that raw fuel is supplied to the reforming burner as combustion fuel.

  That is, the reformed gas generated in the reforming unit is supplied to the fuel cell as a fuel gas for power generation, and the exhaust fuel gas discharged from the fuel cell is in another combustion device different from the reformer burner. The reformed burner is combusted, and raw fuel is supplied as combustion fuel.

  In other words, the exhaust fuel gas discharged from the fuel cell may be supplied to the reformer burner as combustion fuel. However, in the fourth feature configuration, the exhaust fuel gas is different from the reformer burner, such as a boiler. The reforming burner is supplied with raw fuel instead of exhaust fuel gas and burned to the reforming burner.

When comparing the case where the exhaust fuel gas is burned with the reformer burner and the case where the raw fuel is burned, the exhaust fuel gas contains carbon dioxide gas, water vapor, etc., so the air ratio is the same. If so, the amount of combustion exhaust gas is reduced when the raw fuel is burned.
Therefore, when the reforming gas generated in the reforming section is supplied to the fuel cell as the fuel gas for power generation in the state where the raw fuel is burned by the reforming burner, By increasing the supply amount of combustion air so that the oxygen concentration becomes 4-8% and increasing the amount of combustion exhaust gas, the heat transfer ratio from the combustion exhaust gas is reduced, and the heat transfer accompanying the flow of combustion exhaust gas is reduced. Since the decrease in the amount of heat is suppressed, the reforming section can be heated to a temperature suitable for the reforming process, and the other processing section can be adjusted to a temperature suitable for the processing in the other processing section.
Therefore, when the generated hydrogen-containing gas is used as a fuel gas for power generation of a fuel cell, the exhaust fuel gas is burned by another combustion device different from the reforming burner, and the raw fuel is burned by the reforming burner. Even in this case, the hydrogen-containing gas can be appropriately generated so as to have a predetermined composition.

Hereinafter, an embodiment in which the present invention is applied to a hydrogen-containing gas generator for a fuel cell will be described with reference to the drawings.
FIGS. 1 and 2 show a fuel cell power generation apparatus equipped with a hydrogen-containing gas generation apparatus P according to the present invention. This fuel cell power generation apparatus uses hydrogen-based raw fuel gas as a raw material and hydrogen gas as a main component. The hydrogen-containing gas generating device P that generates the fuel gas to be generated, the fuel cell G that is supplied with the fuel gas generated by the hydrogen-containing gas generating device P and generates power, and the control unit as a control means that controls the operation C.

  Since the fuel cell G is well known and will not be described in detail and illustrated briefly, the fuel cell G is, for example, a solid state in which a plurality of cells each having a solid polymer film as an electrolyte layer are provided in a stacked state. The fuel gas is supplied from the hydrogen-containing gas generator P to the fuel electrode of each cell, the air is supplied from the reaction blower 36 to the oxygen electrode of each cell, and the electricity between hydrogen and oxygen is configured. It is configured to generate electricity by chemical reaction.

  The hydrogen-containing gas generation device P includes a desulfurization chamber 1 that desulfurizes hydrocarbon-based raw fuel gas, a steam generation chamber 2 that heats and evaporates supplied water to generate steam, and desulfurizes in the desulfurization chamber 1. A reforming chamber 3 as a reforming section for reforming the treated raw fuel gas using the steam generated in the steam generating chamber 2 to generate a reformed processing gas mainly composed of hydrogen gas; A combustion chamber 6 as a combustion section that heats the reforming chamber 3 so that the reforming chamber 3 can be reformed by burning the combustion fuel in the quality burner 17, and the reforming process gas supplied from the reforming chamber 3 A conversion chamber 4 for converting carbon monoxide gas into carbon dioxide gas using steam, and a selection for selectively oxidizing the carbon monoxide gas remaining in the reforming gas supplied from the conversion chamber 4 Consists of an oxidation chamber 5 and the like, and contains hydrogen with a low carbon monoxide gas content. It is arranged to generate a gas.

  Further, the reforming chamber heating flow chamber 7 for heating the reforming chamber 3 by passing the reforming process gas discharged from the reforming chamber 3, and the combustion chamber 6. Exhaust gas exhaust chamber 8 for heating and heating the steam generation chamber 2 by the exhaust gas so that the steam generation chamber 2 can generate steam, and combustion discharged from the exhaust gas flow chamber 8 for heating The desulfurization chamber is heated by the temperature-controlled exhaust gas flow chamber 9 for adjusting the temperature of the shift chamber 4 with the combustion exhaust gas and the hot reforming gas discharged from the reforming chamber heating flow chamber 7. The desulfurized raw fuel heat exchanger Ea that heats the desulfurized raw fuel gas desulfurized in 1, and the desulfurized raw fuel heat exchanger Ea enters the desulfurization chamber 1 by the reformed gas after heat exchange in the raw heat exchanger Ea. Heat exchanger Eb for raw fuel before desulfurization for heating raw fuel gas to be desulfurized, Beauty, is provided with economizer Ec for recovering exhaust heat of the combustion exhaust gas discharged from the temperature control waste gas flow chamber 9 to the combustion air supplied to the reformer burner 17.

  That is, the temperature of the combustion exhaust gas discharged from the combustion chamber 6 is adjusted so that the steam generation chamber 2 can generate steam, and after the temperature of the steam generation chamber 2 is adjusted, the conversion chamber 4 can be subjected to a modification process. The steam generation chamber 2 and the shift chamber 4 are provided as other processing units for allowing the combustion exhaust gas of the reforming burner 17 discharged from the combustion chamber 6 to flow for temperature control. It is.

  The desulfurized raw fuel heat exchanger Ea is connected to the upstream heat exchange flow chamber 10 through which the reforming gas discharged from the reforming chamber heating flow chamber 7 flows, and the desulfurization chamber 1. The desulfurized raw fuel flow chamber 11 through which the desulfurized raw fuel gas that is desulfurized and supplied to the reforming chamber 3 flows is provided so as to be able to exchange heat, and the raw fuel heat exchange section Eb before desulfurization is provided. Includes a downstream heat exchange flow chamber 12 through which the reformed gas discharged from the upstream heat exchange flow chamber 10 flows, and a raw fuel gas to be desulfurized in the desulfurization chamber 1. The raw fuel flow passage 13 before desulfurization is provided so as to be capable of heat exchange.

  The economizer Ec allows the exhaust heat source exhaust gas flow chamber 14 through which the combustion exhaust gas discharged from the temperature control exhaust gas flow chamber 9 flows and the combustion air supplied to the reforming burner 17. The combustion air flow chamber 16 is configured to be able to exchange heat.

  In this embodiment, as shown in FIG. 12, the exhaust fuel gas discharged from the fuel cell G is combusted in a boiler 44 as another combustion device different from the reforming burner 17. The raw fuel gas is supplied to the reforming burner 17 as a combustion fuel.

As shown in FIG. 2, the hydrogen-containing gas generation device P arranges a plurality of flat containers B that form a processing chamber S for processing a fluid in a laterally stacked manner, and arranges the plurality of containers B in a container arrangement direction. Are pressed by pressing means (not shown) from both sides of the container arrangement direction in a state allowing relative movement in a direction orthogonal to the container.
As shown in FIGS. 3 to 5, the container B includes a pair of container forming members 51 positioned in the container arranging direction by welding the peripheral portions thereof. At least one of them is formed in a dish shape in which the central portion bulges with the peripheral portion as a connection allowance.

  And, by the plurality of processing chambers S formed in the plurality of containers B, the desulfurization, steam generation, reforming, transformation, selective oxidation, combustion chambers 1, 2, 3, 4, 5, 6, and The reforming chamber heating, heating exhaust gas, temperature control exhaust gas, upstream heat exchange, post-desulfurization raw fuel, downstream heat exchange, pre-desulfurization raw fuel, exhaust heat source exhaust gas, combustion fuel, combustion air Each flow chamber 7, 8, 9, 10, 11, 12, 13, 14, 15, 16 is configured.

In this embodiment, the plurality of containers B are formed so that each of the pair of container forming members 51 is the dish-shaped container forming member 51, and is partitioned between the pair of container forming members 51. The peripheral portion is welded and connected with the member 52 positioned, and the processing chamber S is provided on both sides of the partition member 52.
Then, one dish-shaped auxiliary container forming member 53 for positioning a part of the plurality of containers B on the back part of the dish-shaped container forming member 51 in a stacked state is the back part of the peripheral part adjacent thereto. Are formed into a multi-treatment chamber type container Bm in which a plurality of treatment chambers S are formed in the container arrangement direction. This multi-processing chamber type container Bm is shown in FIGS. 4 and 5. The remaining part of the plurality of containers B is a basic container Bs without the auxiliary container forming member 53. This basic type container Bs is shown in FIG.

  The dish-shaped container forming member 51, the partition member 52, and the dish-shaped auxiliary container forming member 53 are each made of a heat-resistant metal such as stainless steel, and the dish-shaped container forming member 51 and the dish-shaped auxiliary container forming member 53 is formed by press-molding a plate made of the heat-resistant metal into a dish shape.

In this embodiment, seven containers B are arranged to constitute the hydrogen-containing gas generation device P.
In addition, in order to clarify the distinction of the seven containers B, for the sake of convenience, reference numerals 1, 2, 3... 7 indicating the arrangement order from the left in FIG. .

  In this embodiment, the first container B1, the second container B2, the fourth container B4, and the rightmost container B7 from the left are the basic containers Bs.

  Further, as shown in FIG. 4, the third container B3 from the left is the auxiliary container forming member 53 on the back of the right dish-shaped container forming member 51 of the pair of dish-shaped container forming members 51. , A multi-processing chamber type container Bm having three processing chambers S arranged in the container alignment direction, and the fifth container B5 from the left is a pair of dishes as shown in FIG. The auxiliary container forming member 53 is provided on each of the backs of the container-shaped container forming member 51 to form a multi-processing chamber type container Bm having four processing chambers S arranged in the container arranging direction. Similarly to the fifth container B5 from the left, the individual container B6 is also a multi-processing chamber type container Bm provided with four processing chambers S arranged in the container arrangement direction.

  As shown in FIG. 2, in the leftmost container B1 (basic container Bs), the exhaust heat source exhaust gas flow chamber 14 is configured in the left processing chamber S, and the combustion air is processed in the right processing chamber S. The flow chamber 16 is configured, and the economizer Ec is configured by the leftmost container B1.

The exhaust gas flow chamber 8 for heating is configured in the left processing chamber S in the second container B2 from the left (basic-type container Bs having two processing chambers S in the container arrangement direction). The steam generation chamber 2 is configured in the processing chamber S.
The steam generation chamber 2 is configured such that the reforming water is supplied from the lower end and the generated steam is discharged from the upper end, and the temperature of the upper end in the steam generation chamber 2 is detected. A water vapor generation temperature sensor Ts is provided.

  As shown in FIG. 4, in the third container B3 from the left (multi-processing chamber type container Bm having three processing chambers S in the container arrangement direction), the combustion chamber is disposed in the processing chamber S at the left end. 6, the reforming chamber 3 is configured by the central processing chamber S, and the reforming chamber heating flow chamber 7 is configured by the rightmost processing chamber S.

  Then, in the central processing chamber S of the third container B3 from the left, ruthenium, nickel, platinum, etc. for reforming the hydrocarbon-based raw fuel gas into a gas mainly composed of hydrogen gas using water vapor The reforming catalyst 19 is filled, and the processing chamber S is formed in the reforming chamber 3.

The reforming chamber 3 is configured such that the raw fuel gas and water vapor are supplied from the upper end in a mixed state and flow downward, and the reforming chamber 3 and the reforming chamber 3 are configured to flow. A fluid passage 54 is provided at the lower end of the dish-like container forming member 51 that separates the processing chamber S that constitutes the flow chamber 7 for heating the quality chamber, and communicates with the processing chambers S adjacent in the container arrangement direction. The reforming process gas that has been reformed in the reforming chamber 3 is caused to flow into the reforming chamber heating flow chamber 7 through the fluid passage portion 54.
A reforming temperature sensor Tr is provided so as to detect the temperature of the reforming reaction catalyst 19 at the lower end portion of the reforming chamber 3.

  Incidentally, in the reforming chamber 3, when the raw fuel gas is a natural gas-based city gas (13A) containing methane gas as a main component, for example, 600 to 750 ° C. due to the catalytic action of the reforming reaction catalyst 19. Under the reforming treatment temperature in the range, methane gas and water vapor are reformed by the following reaction formula (1) to produce a reforming treatment gas mainly composed of hydrogen gas.

Further, the reforming burner is burned in the combustion chamber 6 at the lower end portion in the combustion chamber 6 constituted by the leftmost processing chamber S of the third container B3 from the left. 17 is provided.
As shown in FIG. 4, the reforming burner 17 is configured by forming a plurality of ejection holes 17 a in a row in a longitudinal direction in a cylindrical ejection pipe.
Further, a combustion catalyst holding body 18 holding a combustion catalyst made of platinum, palladium or the like is disposed above the reforming burner 17 in the combustion chamber 6.
A combustion temperature sensor Tf is provided so as to detect the temperature in the combustion chamber 6.

  The reforming burner 17 is supplied with the same raw fuel gas as that supplied to the reforming chamber 3 as combustion fuel in a premixed state with combustion air, so that the reforming burner 17 is ejected from the ejection hole 17a and burned. It is configured.

  The upstream side heat exchange flow chamber 10 is configured in the left processing chamber S of the fourth container B4 (basic type container Bs) from the left, and the desulfurized raw fuel is passed in the right processing chamber S. The flow chamber 11 is constituted, and the fourth vessel B4 from the left constitutes the heat exchanger Ea for raw fuel after desulfurization.

As shown also in FIG. 5, in the fifth container B5 from the left (multi-processing chamber type container Bm having four processing chambers S in the container arrangement direction), the second processing chamber from the left end and the left. Each of S is filled with a desulfurization reaction catalyst 20 for desulfurizing a hydrocarbon-based raw fuel gas to constitute a desulfurization chamber 1, and the third treatment chamber S from the left is a raw fuel flow chamber 13 before desulfurization. The rightmost processing chamber S is configured in the shift chamber 4 by filling it with an iron oxide-based or copper-zinc-based shift reaction catalyst 21 that converts carbon monoxide gas into carbon dioxide gas using water vapor. It is.
Incidentally, although details will be described later, since the transformation chamber 4 constituted by the fifth container B5 from the left is the first stage and the transformation chamber 4 is provided in four stages, the fifth container from the left will be described below. The conversion chamber 4 configured in B5 may be referred to as the first-stage conversion chamber 4.

  Further, the dish-shaped container forming member 51 that partitions the leftmost processing chamber S and the second processing chamber S from the left, the second processing chamber S from the left and the third processing chamber S from the left. Each of the partition members 52 is provided with a fluid passage portion 54 that communicates with the processing chambers S on both sides. Then, the desulfurization chamber 1 configured by the second processing chamber S from the left is the first stage, the desulfurization chamber 1 configured by the leftmost processing chamber S is the second stage, and the raw fuel gas to be desulfurized is After passing through the raw fuel flow chamber 13 before desulfurization and preheating, each desulfurization chamber 1 is flowed in the order of the first stage and the second stage to perform desulfurization treatment.

In addition, a plate-shaped container forming member 51 that partitions the third processing chamber S from the left that constitutes the raw fuel flow chamber 13 before desulfurization and the rightmost processing chamber S that constitutes the first-stage transformation chamber 4 is transmitted. As the heat walls, the raw fuel gas to be desulfurized flowing through the raw fuel flow chamber 13 before desulfurization and the reformed gas to be converted to flow through the first-stage shift chamber 4 are heated through the heat transfer wall. It is configured to be exchanged.
That is, the first-stage transformation chamber 4 is configured to be used as the downstream heat exchange flow chamber 12, and the raw fuel flow chamber 13 before desulfurization and the downstream heat exchange flow chamber 12 The heat exchanger Eb for raw fuel before desulfurization is configured.

  In the sixth container B6 from the left (multi-processing chamber type container Bm having four processing chambers S in the container arrangement direction), the leftmost processing chamber S is configured as the temperature control exhaust gas flow chamber 9; Each of the second chamber from the left, the third chamber from the left, and the rightmost processing chamber S is configured in the shift chamber 4 by being charged with the shift reaction catalyst 21.

  Further, a partition member 52 that partitions the second processing chamber S from the left and the third processing chamber S from the left, and a dish-like container that partitions the third processing chamber S from the left and the rightmost processing chamber S are formed. Each member 51 is provided with a fluid passage portion 54 communicating with the processing chambers S on both sides. The transformation chamber 4 constituted by the second processing chamber S from the left is the second stage, the transformation chamber 4 constituted by the third processing chamber S from the left is the third stage, and the rightmost processing chamber. The transformation chamber 4 constituted by S is assumed to be the fourth stage, and an external gas processing flow path from the first transformation chamber 4 constituted by the fifth container B5 from the left to the second transformation chamber 4 is provided. The reforming process gas is supplied at 32, and the reforming process gas is passed through the shift chambers 4 in the order of the second, third, and fourth stages to perform the shift process.

  The second-stage shift chamber 4 adjacent to the temperature control exhaust gas flow chamber 9 is supplied with reforming process gas from the first-stage shift processing chamber 4 from the upper end, flows downward, and moves to the lower end. It is configured to be discharged toward the third-stage shift chamber 4 from the fluid passage section 54 of the first section, and the shift is performed so as to detect the temperature of the shift reaction catalyst 21 at the upper end in the second-stage shift chamber 4. A temperature sensor Tt is provided.

  Incidentally, in the shift chamber 4, carbon monoxide and water vapor in the reformed gas supplied from the reforming chamber 3 are, for example, in the range of 150 to 400 ° C. by the catalytic action of the shift reaction catalyst 21. Under the modification treatment temperature, the modification reaction is performed according to the following reaction formula (2).

  In the seventh container from the left, that is, the rightmost container B7 (basic container Bs), the left processing chamber S is used for heat transfer adjustment without using anything, and the right processing chamber S contains carbon monoxide gas. The selective oxidation chamber 5 is configured by filling a selective oxidation catalyst 22 made of a noble metal such as platinum, ruthenium, or rhodium that is selectively oxidized.

  The selective oxidation chamber 5 is supplied from the lower end portion in a mixed state with the reforming process gas transformed in the shift chamber 4 and the selective oxidation air, flows upward, and is discharged from the upper end portion. The selective oxidation temperature sensor Tm is provided so as to detect the temperature of the selective oxidation catalyst 22 at the substantially central portion in the vertical direction in the selective oxidation chamber 5.

  Incidentally, in the selective oxidation chamber 5, the catalytic action of the selective oxidation reaction catalyst 22, for example, remains in the reformed treatment gas after the shift treatment at a selective oxidation treatment temperature of 80 to 150 ° C. Carbon oxide gas is selectively oxidized.

  When the processing chamber S of the container B is filled with a catalyst such as the reforming reaction catalyst 19 or the like, it is slightly above the bottom of the processing chamber S in a posture in which the flat container B is vertically aligned. In order to receive the catalyst at the section, the porous catalyst receiving plate 55 is attached by welding to the dish-shaped container forming member 51, the partition member 52 or the dish-shaped auxiliary container forming member 53 forming the processing chamber S. is there.

  Then, in the posture in which the above-described seven flat containers B are arranged in the vertical direction, the left side of the left end container B1 and the left end container B1 and the second container B2 from the left, Between the second container B2 and the third container B3 from the left, between the third container B3 from the left and the fourth container B4 from the left, and the fourth container B4 from the left In a state where the heat transfer amount adjusting heat insulating material 23 is arranged between the fifth container B5 from the left and between the fifth container B5 from the left and the sixth container B6 from the left. Arranged in close contact, and configured to press the seven containers B in close contact from both sides in the container alignment direction in a state allowing relative movement in a direction orthogonal to the container alignment direction, The side of the rightmost container B7 constituting the selective oxidation chamber 5 is ventilated toward the container B7. Sea urchin and the cooling fan 26 is provided, the by cooling fan 26, is arranged to cool the selective oxidation chamber 5.

That is, among the desulfurization chamber 1, the reforming chamber 3, the shift chamber 4, and the selective oxidation chamber 5, the reforming chamber 3 needs to be maintained at the highest temperature, and the selective oxidation chamber 5 needs to be maintained at the lowest temperature.
Therefore, the reforming chamber 3 and the combustion chamber 6 that heats the reforming chamber 3 are provided in close contact with each other so that heat can be transferred. The chamber 4 and the selective oxidation chamber 5 are arranged side by side from the reforming chamber 3 in the order described, and are provided in a state where heat can be transferred from the reforming chamber 3 and the combustion chamber 6, and the reforming chamber 3 and the combustion chamber 6 are in close contact with each other. The steam generation chamber 2 is provided on the combustion chamber 6 side in such a state that heat can be transferred from the reforming chamber 3 and the combustion chamber 6.

  And between adjacent ones, that is, between the reforming chamber 3 and the desulfurization chamber 1, between the desulfurization chamber 1 and the shift chamber 4, between the shift chamber 4 and the selective oxidation chamber 5, and the combustion chamber. The heat transfer state (heat transfer amount) between the steam generator 6 and the steam generation chamber 2 is set to a predetermined value, and the combustion amount of the reforming burner 17 is adjusted so as to maintain the reforming chamber 3 at the reforming temperature. In addition, by adjusting the flow rate of the cooling fan 26 so as to maintain the selective oxidation chamber 5 at the selective oxidation treatment temperature, the desulfurization chamber 1 and the shift chamber located between the reforming chamber 3 and the selective oxidation chamber 5 are controlled. The chamber 4 can be maintained at a desulfurization treatment temperature and a modification treatment temperature, respectively, and the steam generation chamber 2 can be maintained at a temperature suitable for steam generation.

  Hereinafter, the connection form of the flow path with respect to each processing chamber S for supplying the fluid to each processing chamber S formed in each container B and discharging the fluid from each processing chamber S will be described. In each processing chamber S, the fluid is supplied from the upper part and flows downward and discharged from the lower part, or the fluid is supplied from the lower part and flows upward and supplied from the upper part. Since the fluid is configured to flow in the vertical direction so as to be discharged, each flow path is connected to the upper end portion or the lower end portion of each processing chamber S.

  A raw fuel supply passage 31 for power generation is connected to the raw fuel flow chamber 13 before desulfurization, and the second stage desulfurization chamber 1 and the raw fuel flow chamber 11 after desulfurization are connected to the raw fuel flow chamber 11 after desulfurization. The reforming chamber 3, the reforming chamber heating flow chamber 7 and the upstream heat exchange flow chamber 10, and the upstream heat exchange flow chamber 10 and the downstream heat exchange. The first-stage conversion chamber 4 that also serves as the flow-through chamber 12, the first-stage conversion chamber 4 and the second-stage conversion chamber 4, and the fourth-stage conversion chamber 4 and the selective oxidation And the selective oxidation chamber 5 and the fuel gas supply part of the fuel cell G are connected by a fuel gas flow path 33 so that the raw fuel flow before desulfurization is connected. Chamber 13, first-stage desulfurization chamber 1, post-desulfurization raw fuel flow chamber 11, reforming chamber 3, reforming chamber heating flow chamber 7, upstream heat exchange flow chamber 10, 1 2nd stage , 3-stage, 4-stage shift chamber 4, flows through the selective oxidation chamber 5 in order, it is formed a gas processing route to the fuel cell G.

  The power generation raw fuel supply path 31 includes a power generation raw fuel control valve V1 that adjusts the supply amount of the reforming raw fuel gas supplied through the power generation raw fuel supply path 31, and the power generation raw fuel supply path 31. A power generation raw fuel flow rate sensor Q for detecting the flow rate of the raw fuel gas flowing through the power generation raw fuel supply path 31 after the supply amount is adjusted by the fuel control valve V1 is provided.

  In the gas processing flow path 32 connecting the second-stage desulfurization chamber 1 and the desulfurized raw fuel flow chamber 11, an ejector 35 for mixing water vapor into the desulfurized raw fuel gas is provided.

  Further, the selective oxidation air is supplied from the selective oxidation blower 24 as the selective oxidation blower means to the gas processing flow path 32 connecting the fourth stage conversion chamber 4 and the selective oxidation chamber 5. An oxidizing air supply path 25 is connected, and the selective oxidizing air is mixed with the reforming gas that has been subjected to the transformation treatment in the transformation chamber 4 and supplied to the selective oxidation chamber 5.

That is, the raw fuel gas is desulfurized in the first-stage and second-stage desulfurization chambers 1, and the steam supplied from the steam generation chamber 2, which will be described later, is supplied to the desulfurized raw fuel gas through the steam flow path 34. The raw fuel gas mixed with the ejector 35 and mixed with the water vapor is reformed in the reforming chamber 3, and the reformed gas is supplied to the first, second, third, and fourth stages. A shift treatment is performed in the shift chamber 4 and the reformed reformed gas is selectively oxidized in the selective oxidation chamber 5 to generate a hydrogen-containing gas having a low carbon monoxide content. The hydrogen-containing gas is used as a fuel. The gas is supplied to the fuel cell G through the fuel gas passage 33 as gas.
In this embodiment, as shown in FIG. 12, the hydrogen-containing gas generated by the hydrogen-containing gas generator P is supplied as fuel gas to a plurality (three in this embodiment) of fuel cells G. It is.

  As shown in FIG. 2, the combustion chamber 6 and the heating exhaust gas passage chamber 8, the heating exhaust gas passage chamber 8 and the temperature adjustment exhaust gas passage chamber 9, and the temperature adjustment exhaust gas passage chamber. 9 and the exhaust heat source exhaust gas flow chamber 14 of the economizer Ec are connected to each other by a combustion exhaust gas flow path 37, and the combustion exhaust gas discharged from the combustion chamber 6 is heated to the exhaust gas flow chamber 8 for heating and temperature control. The exhaust gas flow chamber 9 and the exhaust heat source exhaust gas flow chamber 14 of the economizer Ec are passed in this order.

Also, a combustion blower 39 serving as a combustion blower for supplying combustion air to the reforming burner 17 and the combustion air flow chamber 16 of the economizer Ec are connected to the combustion air flow chamber 16 and the combustion air flow chamber 16. The reforming burner 17 is connected to each other by a combustion air flow path 40.
Then, in the economizer Ec, the exhaust heat of the combustion exhaust gas is recovered into combustion air, the combustion air is preheated, and the preheated combustion air is supplied to the reforming burner 17 for combustion. It is constituted as follows.

Further, the reformer burner 17 is connected with a burner raw fuel supply passage 41 for supplying the same raw fuel gas as the reforming raw fuel gas as a combustion fuel.
The burner raw fuel supply passage 41 is provided with a burner raw fuel control valve V2 for adjusting the supply amount of the burner raw fuel gas supplied through the burner raw fuel supply passage 41.

  The burner raw fuel supply path 41 and the combustion air flow path 40 are connected to the reforming burner 17 in a state of being joined before the reforming burner 17, The reformer burner 17 is configured to be premixed with the combustion air.

  A reforming water supply passage 43 for supplying reforming water for generating steam for reforming treatment by the reforming water pump 42 is connected to the steam generating chamber 2, and the heating exhaust gas flow chamber 8 is used. The steam flow path 34 for guiding the steam generated in the steam generation chamber 2 by heating is connected to the ejector 35.

  That is, the processing chamber S adjacent to the reforming chamber 3 is configured as a combustion chamber 6 that combusts combustion fuel to heat the reforming chamber 3, and one of the two processing chambers S adjacent to each other is formed. An exhaust gas flow chamber for heating, in which the supplied water is vaporized by heating to form the steam generation chamber 2, and the other exhaust gas exhausted from the combustion chamber 6 is passed through to heat the steam generation chamber 2. The steam generated in the steam generation chamber 2 is supplied to the reforming chamber 3 for reforming reaction.

By configuring as described above, the hydrogen-containing gas generation device P that generates a hydrogen-containing gas with a low carbon monoxide gas content using hydrocarbon-based raw fuel and steam is used for the raw fuel reforming process. It is configured integrally with a water vapor generating part that generates water vapor.
Although it is necessary to heat each of the reforming chamber 3 and the steam generation chamber 2, the water is evaporated at a temperature lower than the temperature at which the raw fuel and the steam undergo the reforming reaction, and the combustion chamber 6 is Provided adjacent to the reforming chamber 3, the reforming chamber 3 is heated to a high temperature in the combustion chamber 6, and the combustion exhaust gas discharged from the combustion chamber 6 is flowed through the heating exhaust gas adjacent to the steam generation chamber 2. The steam generation chamber 2 is heated by flowing through the chamber 8.
That is, since the single combustion chamber 6 heats both the reforming chamber 3 and the steam generation chamber 2 to suitable temperatures, it is possible to reduce the cost of the apparatus and reduce the energy consumption.

  As shown in FIG. 12, an offgas passage 38 that guides offgas discharged from the fuel electrode of each fuel cell G is connected to a boiler 44, and offgas discharged from a plurality of fuel cells G is burned in the boiler 44. It is comprised so that it may make.

Next, the control operation of the control unit C will be described.
The control unit C is configured to adjust the amount of fuel supplied to the reforming burner 17 so that the temperature of the reforming chamber 3 becomes a set appropriate temperature.
In the present invention, the control unit C adjusts the amount of combustion air supplied to the reforming burner 17 so that the oxygen concentration in the combustion exhaust gas of the reforming burner 17 is 4 to 8%. In addition, the combustion air to the reforming burner 17 is set so that the temperature of the steam generation chamber 2 becomes the set temperature for generating steam or the temperature of the shift chamber 4 becomes the set temperature for conversion. The supply amount is corrected.
The combustion air supply amount at which the residual oxygen concentration in the combustion exhaust gas is 4 to 8% corresponds to the combustion air supply amount at which the air ratio is in the range of approximately 1.2 to 1.6. The supply amount of combustion air to the reforming burner 17 is adjusted so that the air ratio becomes 1.2 to 1.6.

  Incidentally, in this embodiment, the supply amount of combustion air to the reforming burner 17 is adjusted so that the oxygen concentration in the combustion exhaust gas becomes 6%, that is, the air ratio becomes 1.4. It is constituted as follows.

Hereinafter, the control operation of the control unit C will be specifically described.
As shown in the flowchart of FIG. 6, at the start timing, the control unit C ignites the reforming burner 17 and executes start-up operation processing for heating the reforming chamber 3 to the set temperature for reforming. When the operation process is completed, a normal operation process is performed in which the raw fuel gas for reforming is supplied to the hydrogen-containing gas generation unit P to generate the fuel gas, and the generated fuel gas is supplied to the fuel cell G to generate power. When the stop timing is reached, a predetermined stop process is executed to stop the operation of the hydrogen-containing gas generator P and the fuel cell G.
For example, when the fuel cell power generator is operated during a predetermined operation time of the day, the start timing is reached at the start time of the operation time zone, and the stop timing is reached at the end time of the operation time zone. .
Incidentally, the set temperature for reforming is set to a predetermined reforming processing temperature within a range of 600 to 750 ° C.

Next, the start-up operation process will be described.
Note that a set fuel supply amount for start-up is set as the supply amount of combustion fuel to the reforming burner 17 in the start-up operation process, and the residual oxygen concentration in the combustion exhaust gas is 4 with respect to the set fuel supply amount for start-up. The starting set air supply amount is set within a range of% to 8%.
The combustion air supply amount at which the residual oxygen concentration in the combustion exhaust gas is 4 to 8% corresponds to the combustion air supply amount at which the air ratio is in the range of approximately 1.2 to 1.6. The starting set air supply amount is set within the range of 1.2 to 1.6 with respect to the starting set fuel supply amount.
Incidentally, in this embodiment, the set air supply amount for starting is set so that the residual oxygen concentration in the combustion exhaust gas is 6%, that is, the air ratio is 1.4.

  For example, the starting set fuel supply amount is set to 1 liter / min (standard state), the starting set air supply amount is set to 1.4 (the residual oxygen concentration in the combustion exhaust gas is 6%), 13 It is set to liter / min (standard state).

  As shown in the flowchart of FIG. 7, at the start timing, the rotational speed of the combustion blower 39 is adjusted so that the supply amount of combustion air becomes the start set air supply amount, and an igniter (not shown) is turned on. The opening of the burner raw fuel control valve V2 is adjusted so that the supply amount of the raw fuel gas for the burner becomes the set fuel supply amount for starting, and the reformer burner 17 is adjusted by a frame rod (not shown). When ignition is detected, the igniter is turned off. After that, when the temperature of the reforming reaction catalyst 19 reaches the reforming set temperature (for example, 700 ° C.) based on the detection information of the reforming temperature sensor Tr, start-up operation is performed. The process is terminated and the process returns (steps # 1 to # 6).

The normal operation process will be described.
In this normal operation processing, a target output that follows the currently requested power load is set, and an electric main operation for adjusting the output of the fuel cell G to the target output (output current value) is executed.
As shown in FIG. 9, the flow rate of the raw fuel gas for reforming required to output the target output from the fuel cell G is set according to the target output.
In addition, as shown in FIG. 10, the temperature in the combustion chamber 6 required for maintaining the reforming reaction catalyst 19 at a temperature suitable for the reforming process (for example, the reforming set temperature) is set to a target. It is set according to the output.
In addition, as shown in FIG. 11, the reforming is performed so that a predetermined S / C (ratio of the amount of steam supplied to the amount of raw fuel gas supplied to the reforming chamber 3) is obtained with respect to the raw fuel gas flow rate for reforming. The rotational speed of the reforming water pump 42 for supplying water is set according to the target output.

  As shown in the flowchart of FIG. 8, the control unit C sets a target output that follows the power load, and based on the detection information of the power generation raw fuel flow sensor Q, the control unit C supplies the reforming chamber 3 with reforming. The raw fuel control valve V1 for power generation is adjusted so that the supply flow rate of the raw fuel gas becomes a flow rate corresponding to the target output, and the supply flow rate of the reforming water to the reforming chamber 3 corresponds to the target output. The rotational speed of the reforming water pump 42 is adjusted so that the flow rate becomes, and further, based on the detection information of the combustion temperature detection means Tf, the temperature in the combustion chamber 6 becomes a temperature corresponding to the target output. In order to adjust the supply amount of the raw fuel gas for the burner to the reforming burner 17, the raw fuel control valve V2 for the burner is adjusted, and the raw fuel so adjusted by the raw fuel control valve V2 for the burner is adjusted. The reforming bar is adjusted so that the air ratio is 1.4 with respect to the gas supply. In order to adjust the supply amount of combustion air to 17 to adjust the rotational speed of the combustion air blower 39 (Step # 11 to # 13).

  Specifically, the relationship between the rotational speed of the combustion blower 39 and the air flow rate is set in advance and stored in the control unit C. The control unit C is based on the relationship between the rotational speed and the air flow rate. Then, the rotational speed corresponding to the supply amount of combustion air with an air ratio of 1.4 is obtained, and the combustion blower 39 is controlled so as to be the rotational speed.

Subsequently, at step # 14, based on the detection information of the shift temperature sensor Tt, whether or not the temperature tt of the shift reaction catalyst 21 is equal to or lower than a lower limit temperature obtained by subtracting the shift set temperature range Δt1 from the shift set temperature tts. If it is determined that the temperature is equal to or lower than the lower limit temperature, the supply amount of combustion air is increased and corrected every set time until the temperature tt of the shift reaction catalyst 21 becomes higher than the lower limit temperature. Processing is executed (steps # 14 to # 16).
However, the above-described increase correction of the combustion air supply amount is configured such that the air ratio is within a range of 1.6 or less.

When it is determined in step # 14 that the temperature tt of the shift reaction catalyst 21 is higher than the lower limit temperature, in step # 17, based on the detection information of the shift temperature sensor Tt and the detection information of the water vapor generation temperature sensor Ts. Thus, the temperature tt of the shift reaction catalyst 21 is equal to or higher than the upper limit temperature for shift obtained by adding the shift set temperature range Δt1 to the shift set temperature tts, and the temperature ts in the steam generation chamber 2 is the set temperature tss for steam generation. It is determined whether the temperature tt of the shift reaction catalyst 21 is equal to or higher than the upper limit temperature for shift, and whether the temperature tt of the shift reaction catalyst 21 is equal to or higher than the upper limit temperature for shift. When the temperature ts is equal to or higher than the upper limit temperature for steam generation, the temperature tt of the shift reaction catalyst 21 becomes lower than the upper limit temperature for shift or the temperature ts in the steam generation chamber 2 is higher than the upper limit temperature for steam generation. Until the temperature becomes lower than the limit temperature, a process of reducing and correcting the supply amount of combustion air by a set amount is executed at each set time (steps # 17 to # 19).
However, the above-described reduction correction of the combustion air supply amount is configured so that the air ratio is 1.2 or more.

  In step # 14, it is determined that the temperature tt of the shift reaction catalyst 21 is higher than the lower limit temperature. In step # 17, the temperature tt of the shift reaction catalyst 21 is lower than the upper limit temperature for shift, or When it is determined that the temperature ts in the steam generation chamber 2 is lower than the upper limit temperature for steam generation, the process returns.

  By the way, the set temperature for transformation tts is set within a range of 150 to 400 ° C., and is set to a temperature suitable for the shift treatment, and the set temperature for steam generation tss is used for steam generation in the steam generation chamber 2. The temperature is set to an appropriate temperature, and the set temperature range for transformation Δt1 and the set temperature range for steam generation Δt2 are temperatures at which frequent increase and decrease corrections of combustion air can be suppressed, for example, The set temperature range Δt1 for transformation is set to 5 to 10 ° C., and the set temperature range Δt2 for steam generation is set to 10 to 15 ° C.

[Another embodiment]
Next, another embodiment will be described.
(A) The condition for increasing the combustion air supply amount is not limited to the condition exemplified in the above embodiment, that is, the condition that the temperature tt of the shift reaction catalyst 21 is lower than the lower limit temperature. The temperature tt of 21 is equal to or lower than the lower limit temperature, and the temperature ts in the steam generation chamber 2 is equal to or lower than the lower limit temperature for steam generation obtained by subtracting the set temperature range Δt2 for steam generation from the set temperature tss for steam generation. Or a condition satisfying that the temperature ts in the steam generation chamber 2 is equal to or lower than the lower limit temperature for steam generation.

(B) The conditions for reducing the combustion air supply amount are the conditions exemplified in the above embodiment, that is, the temperature tt of the shift reaction catalyst 21 is equal to or higher than the upper limit temperature for shift, and the steam generation chamber 2 It is not limited to the conditions which satisfy | fill both that the inside temperature ts is more than the upper limit temperature for water vapor | steam production | generation, The conditions which satisfy | fill either one may be sufficient.

(C) In the normal operation in which the raw fuel gas for reforming is supplied to the hydrogen-containing gas generating part P to generate the fuel gas and the generated fuel gas is supplied to the fuel cell G to generate power, the reforming burner 17 The combustion fuel to be supplied is not limited to the same raw fuel gas as the raw fuel gas for reforming as exemplified in the above embodiment.
For example, a gas composed of the off gas of the fuel cell G and the raw fuel gas that is insufficient for the off gas alone to heat the reforming chamber 3 so that the reforming process can be performed may be used.
However, regardless of the type of combustion fuel, the amount of combustion air supplied to the reforming burner 17 is adjusted so that the oxygen concentration in the combustion exhaust gas of the reforming burner 17 is 4-8%.

(D) In adjusting the amount of combustion air supplied to the reforming burner 17 so that the residual oxygen concentration in the combustion exhaust gas is 4 to 8%, the air ratio is 1. In place of the configuration in which the amount of combustion air supplied to the reforming burner 17 is adjusted to be 2 to 1.6, an oxygen concentration sensor for detecting the oxygen concentration in the combustion exhaust gas of the reforming burner 17 is provided. A configuration may be employed in which the amount of combustion air supplied to the reforming burner 17 is adjusted based on the detection information of the oxygen concentration sensor.

(E) Other processing units different from the reforming unit 3 are not limited to the steam generation chamber 2 and the conversion chamber 4 exemplified in the above embodiment. For example, the desulfurization chamber 1 and the selective oxidation chamber 5 are not limited thereto. But it ’s okay.

(F) The combustion equipment for burning off-gas from the fuel cell G is not limited to the boiler exemplified in the above embodiment, and may be, for example, a burner for heating various furnaces.

(G) The hydrocarbon-based raw fuel is not limited to the natural gas-based city gas (13A) exemplified in the above embodiment, and various kinds of fuels such as alcohols such as propane gas and methanol are used. Can be used.

(H) The hydrogen-containing gas generator according to the present invention can be used for various purposes other than for generating fuel gas to be supplied to the fuel cell as exemplified in the above embodiment.

Block diagram of a fuel cell power generator equipped with a hydrogen-containing gas generator Longitudinal cross section of hydrogen-containing gas generator Perspective view of container Perspective view of container Perspective view of container The figure which shows the flowchart of control action The figure which shows the flowchart of control action The figure which shows the flowchart of control action Diagram showing the relationship between target output and raw fuel gas flow rate Diagram showing the relationship between target output and combustion chamber temperature The figure which shows the relationship between the target output and the rotation speed of the reforming water pump The figure which shows the whole schematic structure of a fuel cell power generator

Explanation of symbols

2 Steam generation unit, other processing unit 3 Reforming unit 4 Transformation unit, other processing unit 6 Combustion unit 17 Reforming burner 44 Other combustion equipment C Control means G Fuel cell

Claims (4)

A reforming section for reforming the supplied hydrocarbon-based raw fuel and steam to generate a reforming treatment gas containing hydrogen gas as a main component;
A combustion unit that burns fuel for combustion in a reformer burner and heats the reforming unit so as to be reformed; and
The combustion exhaust gas of the reforming burner discharged from the combustion unit is configured to flow for temperature control of another processing unit different from the reforming unit,
The control means for controlling the operation is a hydrogen-containing gas generator configured to adjust the amount of combustion fuel supplied to the reforming burner so that the temperature of the reforming section becomes a set appropriate temperature. ,
The control means adjusts the supply amount of combustion air to the reforming burner so that the oxygen concentration in the combustion exhaust gas of the reforming burner is 4 to 8%, and the temperature of the other processing unit A hydrogen-containing gas generating device configured to correct the amount of combustion air supplied to the reforming burner so that becomes a set temperature. As the other processing unit, a water vapor generating unit for heating supplied water to generate water vapor to be supplied to the reforming unit, and carbon monoxide in the reforming treatment gas generated in the reforming unit And a metamorphic part that transforms to carbon,
The flue gas discharged from the combustion section is temperature-controlled so that the steam generation section can generate steam, and after the temperature control of the steam generation section, the conversion section is controlled to be temperature-controllable. Configured to flow,
Combustion air to the reforming burner so that the temperature of the steam generation unit becomes a set temperature for steam generation or the temperature of the shift unit becomes a set temperature for conversion. The hydrogen-containing gas generating device according to claim 1, wherein the hydrogen-containing gas generating device is configured to correct a supply amount of the gas. The steam generation unit is provided on one side of the reforming unit and the combustion unit in a state where heat can be transferred from the reforming unit and the combustion unit,
The hydrogen-containing gas generating device according to claim 2, wherein the transformation unit is provided on the other side of the reforming unit and the combustion unit in a state where heat can be transferred from the reforming unit and the combustion unit. Other combustion equipment in which the reformed gas generated in the reforming unit is supplied to the fuel cell as a fuel gas for power generation, and the exhaust fuel gas discharged from the fuel cell is different from the reforming burner Configured to burn at
The hydrogen-containing gas generation device according to any one of claims 1 to 3, wherein raw gas is supplied as combustion fuel to the reforming burner.

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