JP2008247698A - Hydrogen-containing gas producing apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a hydrogen-containing gas producing apparatus capable of improving stabilization of supply of a hydrogen-containing gas having low carbon monoxide concentration. <P>SOLUTION: The hydrogen-containing gas producing apparatus includes: a reforming section 3; a modifying section 4 in which carbon monoxide gas in reformed gas supplied from the reforming section 3 is converted to carbon dioxide gas and the resultant gas is cooled in a heat exchange part 9 for heat recovery; a combustion heating means 17 to heat the reforming section 3 so that reforming is made possible and to heat the modifying section 4 so that modification is made possible; and a reforming water supply means J to supply reforming water for reforming raw fuel in the reforming section 3, wherein an operation control means C controls the operation of the heating means 17 so that the temperature of the reforming section 3 is kept in a set proper range for reforming, and when the temperature of the conversion section 4 becomes higher than a set proper range for conversion, the operation control means C controls the operation of the reforming water supply means J so that the supply of reforming water is increased to increase a steam/carbon ratio which is a ratio of the amount of steam to the amount of raw fuel. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

The present invention includes a reforming unit that reforms a hydrocarbon-based raw fuel to generate a reformed gas containing hydrogen gas as a main component;
A transformation section that transforms carbon monoxide gas in the reforming gas supplied from the reforming section into carbon dioxide gas and is cooled in a heat exchange section for heat recovery;
Heating means for heating the reforming part so as to allow a reforming process and heating the metamorphic part so as to allow a modification process;
Reforming water supply means for supplying reforming water for reforming raw fuel in the reforming section;
The present invention relates to a hydrogen-containing gas generation device provided with an operation control means for controlling the operation.

  Such a hydrogen-containing gas generating apparatus is configured to heat the reforming section so that the reforming process can be performed by the combustion-type heating means and to heat the metamorphic section so that the modification process can be performed. The raw fuel is reformed using steam to a reforming gas containing hydrogen gas as a main component, and the carbon monoxide gas in the reforming gas supplied from the reforming unit is converted into carbon dioxide gas at the shift unit. The hydrogen-containing gas having a low carbon monoxide gas concentration is generated by the modification treatment, and the generated hydrogen-containing gas is used, for example, as a fuel gas for a power generation reaction in a fuel cell.

  By the way, in such a hydrogen-containing gas generating device, the heating amount of the heating means is adjusted to heat the reforming section so that the reforming process is appropriately performed, and the transforming section is transformed by the heating means at the start-up. Although it is heated so that it can be treated, the transformation reaction is an exothermic reaction, so after being heated so that it can be transformed at start-up, it is cooled so that it can be transformed in the heat exchange section for heat recovery. Will be. Incidentally, as a heat exchanging section for heat recovery, for example, a flow section for allowing the raw fuel supplied to the reforming section to flow therethrough is provided so as to be able to conduct heat with the shift section, and the heat generated from the shift section is transferred to the raw fuel. Configured to be collected.

  As described above, the metamorphic section is maintained in a temperature range suitable for performing the metamorphic treatment by being cooled by the heat exchanging section for heat recovery while being heated by the heating means during operation. Therefore, the temperature is likely to change due to fluctuations in the outside temperature, and in particular, since the metamorphic reaction in the metamorphic part is an exothermic reaction, the temperature of the metamorphic part tends to be high, and If the temperature is higher than an appropriate range in which the shift treatment can be appropriately performed, the shift reaction becomes difficult to occur, so that the carbon monoxide concentration of the generated hydrogen-containing gas may be increased.

Therefore, in such a hydrogen-containing gas generation device, conventionally, the operation control means has been such that the temperature of the reforming section is lower than the appropriate range for the reforming process, and the temperature of the shift section is lower than the appropriate range for the shift process. Is increased, the fuel supply amount to the combustion type heating means is adjusted to increase and the combustion air supply amount is adjusted to decrease, so that the air-fuel ratio of the combustion type heating means is lowered and the temperature of the reforming section is increased. When the temperature becomes higher than the proper range for the reforming process and the temperature of the shift section becomes higher than the proper range for the shift process, the fuel supply amount and the combustion air supply amount to the combustion type heating means are decreased and adjusted. Was configured.
In other words, the temperature of each of the reforming section and the shift section is maintained in an appropriate range by adjusting the air-fuel ratio of the combustion type heating means by the operation control means (see, for example, Patent Document 1). .)

Although not described in the above-mentioned Patent Document 1, the operation control means performs combustion when the temperature of the reforming section is in the proper range for the reforming process and the temperature of the shift section becomes higher than the proper range for the transforming process. It is believed that the combustion air supply to the heating means of the formula is configured to increase.
That is, it is considered that the temperature of the metamorphic portion is lowered by increasing the air-fuel ratio of the combustion type heating means and lowering the temperature of the combustion exhaust gas.

Table 03/078311

  However, the conventional hydrogen-containing gas generator is configured to maintain the temperature of the metamorphic section in an appropriate range by adjusting the air-fuel ratio of the combustion-type heating means. If the air-fuel ratio of the combustion-type heating means is adjusted to maintain the combustion-type heating means, the combustion state of the combustion-type heating means becomes unstable, and the reforming process in the reforming section becomes unstable. There is a possibility that the generation of a hydrogen-containing gas having a low carbon monoxide concentration becomes unstable.

  This invention is made | formed in view of this situation, The objective is to provide the hydrogen containing gas production | generation apparatus which can improve stabilization of hydrogen containing gas production | generation of a low carbon monoxide density | concentration.

The hydrogen-containing gas generation device of the present invention includes a reforming unit that reforms a hydrocarbon-based raw fuel to generate a reformed gas containing hydrogen gas as a main component,
A transformation section that transforms carbon monoxide gas in the reforming gas supplied from the reforming section into carbon dioxide gas and is cooled in a heat exchange section for heat recovery;
Combustion-type heating means for heating the reforming part so as to allow a reforming process and heating the metamorphic part so as to allow a modification process;
Reforming water supply means for supplying reforming water for reforming raw fuel in the reforming section;
An operation control means for controlling the operation, and
In the first characteristic configuration, the operation control unit controls the operation of the heating unit so that the temperature of the reforming unit falls within a setting appropriate range for the reforming process, and the temperature of the transforming unit is When higher than the appropriate setting range, the operation of the reforming water supply means is controlled so as to increase and adjust the supply amount of reforming water so as to increase the steam / carbon ratio, which is the ratio of the amount of steam to the raw fuel. It is characterized by being configured as described above.

  That is, the operation control means controls the operation of the heating means so that the temperature of the reforming section is within the set appropriate range for the reforming process, and the temperature of the shift section is higher than the set appropriate range for the transforming process. Then, the operation of the reforming water supply means is controlled so as to increase and adjust the supply amount of the reforming water so as to increase the steam / carbon ratio, which is the ratio of the amount of steam to the raw fuel.

In other words, since the production amount of the hydrogen-containing gas needs to be a predetermined target production amount, the supply amount of the raw fuel is adjusted to the predetermined target supply amount. Therefore, by increasing the supply amount of water vapor This will increase the water vapor / carbon ratio.
When the supply amount of raw fuel is adjusted to a predetermined target supply amount and the supply amount of steam is increased to increase the steam / carbon ratio, the mixed gas of raw fuel and steam supplied to the reforming unit Therefore, the operation of the combustion-type heating means is controlled so that the temperature of the reforming section is within the set appropriate range for the reforming process, and the steam / carbon is increased. As the amount of steam supplied increases to increase the ratio, the amount of the shift gas supplied from the reforming section to the shift section increases, but even if the steam / carbon ratio increases, monoxide in the shift process gas Since the amount of carbon gas is substantially constant and the amount of metamorphic reaction in the metamorphic part is substantially constant, the increase in the amount of the metamorphic treatment gas increases the temperature in the metamorphic part, thereby suppressing the transformation. It is possible to reduce the temperature of the The temperature was brought back parts in setting appropriate ranges for the metamorphic processing can be stably carry out by a modified process in the shift converter.

  Incidentally, the reforming water supply means is configured to heat the reforming water with the combustion exhaust gas of the combustion type heating means to generate steam, and mix the generated steam with the raw fuel supplied to the reforming section. When the heat recovery heat exchanging part is configured to cool the metamorphic part with the combustion exhaust gas of the combustion type heating means used for heating the reforming water in the reforming water supply means, By increasing the water vapor / carbon ratio, that is, increasing the supply amount of reforming water, the amount of heat deprived from the combustion exhaust gas for heating the reforming water increases, so it is supplied to the heat exchanger for heat recovery. As a result, the temperature of the combustion exhaust gas is lowered, so that the cooling capacity of the heat exchanging part for heat recovery can be increased, and the temperature of the metamorphic part can be lowered.

It should be noted that the control of the operation of the combustion type heating means for setting the temperature of the reforming section within the proper setting range for the reforming process is performed while maintaining the air-fuel ratio in a state in which combustion is appropriately performed, This is performed by adjusting the fuel supply amount and the combustion air supply amount to the combustion type heating means so that the temperature falls within the appropriate setting range for the reforming process.
The steam / carbon ratio is set as small as possible in order to improve the efficiency of hydrogen-containing gas generation. Increasing the steam / carbon ratio is advantageous in preventing carbon deposition due to thermal decomposition of the raw fuel. Yes, it is also advantageous for stabilizing the reforming process. Furthermore, even if the steam / carbon ratio is increased, the combustion state of the combustion-type heating means is stable. It is possible to maintain a state in which processing is performed stably.
Therefore, it has become possible to provide a hydrogen-containing gas generator that can improve the stabilization of the generation of a hydrogen-containing gas having a low carbon monoxide concentration.

In addition to the first feature configuration, the second feature configuration is
The reforming unit, a desulfurization unit that desulfurizes the raw fuel supplied to the reforming unit, the shift unit, and a carbon monoxide gas in the reforming process gas supplied from the shift unit are selectively oxidized. A selective oxidation unit is provided between the reforming unit and the selective oxidation unit so that the desulfurization unit and the transformation unit are located, and adjacent ones can conduct heat,
The heating means is provided adjacent to the side of the reforming unit opposite to the side where the desulfurization unit and the transformation unit are provided so as to heat the reforming unit,
A cooling means for cooling the selective oxidation unit is provided;
The operation control unit adjusts the heating amount of the heating unit so that the temperature of the reforming unit becomes the preset temperature for reforming process, and the temperature of the selective oxidation unit becomes the preset temperature for selective oxidation. Further, the present invention is characterized in that the cooling amount of the cooling means is adjusted.

That is, the reforming section, the desulfurization section, the shift conversion section, and the selective oxidation section are provided such that the desulfurization section and the shift conversion section are located between the reforming section and the selective oxidation section, and adjacent ones can conduct heat. The cooling means is provided adjacent to the side of the reforming section opposite to the side where the desulfurization section and the transformation section are provided so that the heating section heats the reforming section. It is done.
The operation control means adjusts the amount of heating of the heating means so that the temperature of the reforming section becomes the preset temperature for reforming treatment, and the cooling means so that the temperature of the selective oxidation section becomes the preset temperature for selective oxidation. In a state where the cooling amount is adjusted, heat is transferred from the reforming unit to the desulfurization unit and the conversion unit, and heat is transferred from the desulfurization unit and the conversion unit to the selective oxidation unit, and heat is released from the selective oxidation unit, thereby desulfurization. The part is heated so that the desulfurization treatment is possible, and the metamorphic part is heated so that the transformation treatment is possible.
The raw fuel desulfurized in the desulfurization section is reformed in the reforming section to generate reformed processing gas, and the carbon monoxide gas in the reforming processing gas supplied from the reforming section in the shift section Is converted to carbon monoxide gas, and further, in the desulfurization section, the carbon monoxide gas in the shift treatment gas supplied from the shift section is selectively oxidized, so that the hydrogen-containing gas in which the carbon monoxide concentration is further reduced Is generated.

That is, for example, city gas as an example of raw fuel contains a sulfur component such as an odorant, and a desulfurization section for desulfurizing the sulfur component may be required. Further, for example, in a polymer type fuel cell, in order to suppress poisoning of the electrode catalyst, a hydrogen-containing gas with a further reduced carbon monoxide concentration is required as a fuel gas for power generation. In applications such as polymer type fuel cells, hydrogen-containing gas with a further reduced carbon monoxide concentration may be desired. For this purpose, selective oxidation treatment that selectively oxidizes carbon monoxide gas in the reformed gas May be provided.
In the reforming treatment temperature in the reforming section, the desulfurization processing temperature in the desulfurization section, the modification processing temperature in the transformation section, and the selective oxidation processing temperature in the selective oxidation section, the reforming treatment temperature is the highest, and the selective oxidation processing temperature. The desulfurization temperature and the shift temperature are between the reforming temperature and the selective oxidation temperature.

  Therefore, the reforming unit, the desulfurization unit, the shift conversion unit, and the selective oxidation unit are disposed between the reforming unit that needs to be maintained at the highest temperature and the selective oxidation unit that needs to be maintained at the lowest temperature. A desulfurization section and a transformation section that need to be maintained at a temperature between the temperature of the selective oxidation section and the temperature of the selective oxidation section are located so as to be able to conduct heat between adjacent ones, and between adjacent ones. By setting the heat coefficient to a predetermined value, the temperature of the desulfurization unit can be set to a temperature at which desulfurization can be performed only by controlling the temperature of each of the reforming unit and the selective oxidation unit to an appropriate temperature. The temperature control configuration of the hydrogen-containing gas generation device is simplified by setting the temperature to a temperature at which the modification treatment is possible.

When the temperature control configuration of the hydrogen-containing gas generator is simplified as described above, the amount of heat transfer from the shift section to the selective oxidation section and from the shift section to the heat exchange section for heat recovery due to disturbances such as fluctuations in the outside air temperature. The amount of heat transfer is likely to fluctuate, and the temperature of the metamorphic part may be higher than the set appropriate range.
Therefore, as described in the first characteristic configuration, when the temperature of the shift unit becomes higher than the appropriate setting range, by increasing the steam / carbon ratio, the reforming process in the reforming unit is performed stably. It is possible to return the temperature of the metamorphic part to the set appropriate range and to stably perform the metamorphic treatment in the metamorphic part.
Therefore, while simplifying the temperature control configuration, hydrogen-containing gas generation that can stably generate a hydrogen-containing gas with a low carbon monoxide concentration from raw material hydrocarbon fuel containing sulfur components as a raw material The device can now be provided.

DESCRIPTION OF EMBODIMENTS Hereinafter, an embodiment in which the present invention is applied to a hydrogen-containing gas generation device 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 hydrogen-containing gas to be generated, the fuel cell G that generates power by supplying the hydrogen-containing gas generated by the hydrogen-containing gas generating device P as a fuel gas, and the operation that controls the operation And a control unit C.

  Since the fuel cell G is well known and will not be described in detail and will be briefly described, the fuel cell G includes, for example, a plurality of cells having a solid polymer film as an electrolyte layer in a stacked state. It is configured as a solid polymer type, fuel gas is supplied from the hydrogen-containing gas generator P to the fuel electrode of each cell, air is supplied from the reaction blower 36 to the oxygen electrode of each cell, and hydrogen and oxygen are mixed. The power generation is performed by an electrochemical reaction.

  The hydrogen-containing gas generation device P includes a desulfurization chamber 1 for desulfurizing a hydrocarbon-based raw fuel gas, and reforming the raw fuel gas desulfurized in the desulfurization chamber 1 to make hydrogen gas a main component. A reforming chamber 3 as a reforming section for generating a quality treatment gas, and a shift section for converting carbon monoxide gas in the reforming process gas supplied from the reforming chamber 3 into carbon dioxide gas using steam As a selective oxidation chamber 5 as a selective oxidation section for selectively oxidizing the carbon monoxide gas remaining in the reforming treatment gas supplied from the conversion chamber 4, and the reforming chamber 3 is heated so that the reforming treatment can be performed and the reforming chamber 4 is heated so as to be capable of the transformation treatment, and the reforming burner 17 serves as a combustion-type heating means. Combustion chamber 6 for combustion and reforming of raw fuel gas in the reforming chamber 3 The reforming water for management is configured to include a reforming water supply unit J such as reforming water supply means for supplying, and is configured to generate a low hydrogen-containing gas concentration of carbon monoxide.

The reforming water supply section J is reformed by heating exhaust gas passage chamber 8 for passing the combustion exhaust gas of reforming burner 17 discharged from the combustion chamber 6 and heating by the heating exhaust gas passage chamber 8. A meandering evaporation process flow path 2 for evaporating water for generating water vapor, and a reforming water pump 42 for supplying the reforming water to the evaporation process flow path 2 and adjusting the supply amount. Has been.
That is, the reforming water supply unit J heats the reforming water with the combustion exhaust gas of the reforming burner 17 to generate steam, and mixes the generated steam with the raw fuel gas supplied to the reforming chamber 3. Is configured to do.

Further, in this hydrogen-containing gas generating device P, a reforming chamber heating flow chamber 7 for heating the reforming chamber 3 by passing the reforming process gas discharged from the reforming chamber 3, the heating chamber A high temperature exhaust gas from the exhaust gas flow chamber 9 for cooling, which cools the shift chamber 4 with the flue gas discharged from the exhaust gas flow chamber 8, and the high temperature gas discharged from the reforming chamber heating flow chamber 7. The desulfurized raw fuel gas heat exchanger Ea that heats the desulfurized raw fuel gas desulfurized in the desulfurization chamber 1 with the reforming treatment gas, and after the desulfurized raw fuel heat exchanger Ea, The heat exchanger Eb for the raw fuel before desulfurization for heating the raw fuel gas to be desulfurized in the desulfurization chamber 1 by the reforming gas and the exhaust heat of the combustion exhaust gas discharged from the cooling exhaust gas flow chamber 9 are modified. Economy recovered to combustion fuel and combustion air supplied to quality burner 17 Ec is provided.
That is, the cooling exhaust gas flow chamber 9 corresponds to a heat recovery heat exchanger for cooling the shift chamber 4.

  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. A 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 undesulfurized raw fuel heat exchanger Eb 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 desulfurized raw fuel flow chamber 13 is configured to be capable of heat exchange.

  Further, the economizer Ec supplies the combustion fuel supplied to the reforming burner 17 on one side of the exhaust heat source exhaust gas flow chamber 14 through which the combustion exhaust gas discharged from the cooling exhaust gas flow chamber 9 flows. A combustion fuel flow chamber 15 to be circulated and a combustion air flow chamber 16 to which the combustion air supplied to the reforming burner 17 is circulated are respectively connected to the exhaust heat source exhaust gas flow chamber 14. It is configured to be able to exchange heat with.

  Further, in this hydrogen-containing gas generating device P, the reforming water tank 44 for storing the reforming water, and the reforming water supplied from the reforming water tank 44 to the evaporation processing flow path 2 is purified to pure water. Water treatment unit 45, for the first stage preheating, in which the reforming water purified to pure water in the water treatment unit 45 is preheated by exchanging heat with the fuel gas supplied from the selective oxidation chamber 5 to the fuel cell G The reforming water preheated in the heat exchanger 46 and the first stage preheating heat exchanger 46 is exchanged with the reforming treatment gas supplied from the shift chamber 4 to the selective oxidation chamber 5 and reformed. A second stage preheating heat exchanger 47 for preheating the quality water is provided.

As shown in FIG. 2, the hydrogen-containing gas generation device P arranges a plurality of flat containers B forming a processing space S for processing a fluid in a laterally stacked manner, and arranges the plurality of containers B in a container arrangement direction. It is configured to be pressed by pressing means (not shown) from both sides of the container arrangement direction in a state that allows relative movement in a direction orthogonal to the container.
As shown in FIGS. 3 to 5, the container B is a state in which the pair of container forming members 51 positioned in the container arranging direction is distributed to both sides of the heat transfer plate 52, and the peripheral portion is the heat transfer plate 52. The heat treatment plate 52 is formed so as to be welded and provided with the processing space S on both sides of the heat transfer plate 52. The pair of container forming members 51 are formed in a shape in which the inner part bulges with the peripheral part as a connection allowance.

By welding one dish-shaped auxiliary container forming member 53, which is positioned in a stacked state on the back part of the container forming member 51, of the plurality of containers B to the back part of the adjacent peripheral part. The multi-processing space type container Bm that forms a plurality of processing spaces S in the container arrangement direction is configured. This multi-processing space type container Bm is shown in FIGS. 4 and 5. The remaining part of the plurality of containers B is a basic type container Bs in which the auxiliary container forming member 53 is not provided. This basic type container Bs is shown in FIG.

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

The desulfurization, reforming, modification, selective oxidation, combustion chambers 1, 3, 4, 5, 6 and the meandering evaporation process are performed by the plurality of processing spaces S formed in the plurality of containers B. Channel 2 and the reforming chamber heating, exhaust gas for heating, exhaust gas for cooling, upstream heat exchange, raw fuel after desulfurization, downstream heat exchange, raw fuel before desulfurization, exhaust heat source exhaust gas, combustion fuel The combustion air flow chambers 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 are configured.
In this embodiment, the hydrogen-containing gas generator P is configured by arranging seven containers B.
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 second container B2, the fourth container B4, and the rightmost container B7 from the left are the basic containers Bs.

  In the leftmost container B1, the auxiliary container forming member 53 is provided on the back of the left container forming member 51 of the pair of container forming members 51, and the three processing spaces S are arranged in the container alignment direction. The third container B3 from the left is the right container forming member 51 of the pair of dish-shaped container forming members 51, as shown in FIG. The auxiliary container forming member 53 is provided on the back, and a multi-processing space type container Bm having three processing spaces S arranged in the container arrangement direction is provided. The fifth container B5 from the left is shown in FIG. 5, the auxiliary container forming member 53 is provided on each of the back portions of the pair of container forming members 51, and the four processing spaces S are arranged in the container alignment direction. And the sixth container B6 from the left is the fifth container from the left. Like the container B5, is a multi-processing space type container Bm having a state arranged four processing space S in the container arrangement direction.

  As shown in FIG. 2, in the leftmost container B1 (multi-processing space type container Bm having three processing spaces S), the combustion fuel flow chamber 15 is configured in the leftmost processing space S, and the center The exhaust heat source exhaust gas flow chamber 14 is configured in the processing space S, the combustion air flow chamber 16 is configured in the rightmost processing space S, and the economizer Ec is configured in the leftmost container B1. Has been.

The exhaust gas flow chamber 8 for heating is configured in the left processing space S in the second container B2 from the left (basic-type container Bs having two processing spaces S in the container arrangement direction), and the right side In the processing space S, the meandering evaporation processing flow path 2 is configured.
An electric heater 27 for auxiliary heating for water vapor generation is provided in a state of being applied to the flow path forming body 56 that forms the evaporation processing flow path 2 in the container B2.

Based on FIG. 3, description is added about this container B2. 3A is a perspective view of the container B2, and FIG. 3B is a vertical side view of the container B2.
One of the pair of container forming members 51 is configured as a flow path forming body 56 having a meandering bulged portion 56 b, and the other is configured as a dish-shaped flow chamber forming body 57.
The bulging portion 56b is provided in the flow path forming body 56 so as to meander from the lower side to the upper side, and the flow path forming body 56 includes a peripheral portion thereof and an adjacent bulging in the bulging portion 56b. In a state where the corresponding portions are welded between the portions, the portions are welded to the heat transfer plate 52, and meandering from below to above between the heat transfer plate 52 and the flow path forming body 56. The evaporation process flow path 2 extending in the direction is formed.
The evaporation treatment flow path 2 is filled with stainless wool 58 for promoting heat transfer.

The flow chamber forming body 57 is welded and connected to the heat transfer plate 52 in a state in which a peripheral portion thereof is welded, and the heating chamber forming body 57 is interposed between the heat transfer plate 52 and the flow chamber forming body 57. An exhaust gas flow chamber 8 is formed.
Further, a plurality of baffle plates 59 are disposed in the heating exhaust gas flow chamber 8 so that the combustion exhaust gas flows in a meandering manner along the serpentine evaporation treatment flow path 2.

As shown also in FIG. 4, in the third container B3 from the left (multi-processing space type container Bm provided with three processing spaces S in the container arrangement direction), the combustion chamber in the leftmost processing space S 6, the reforming chamber 3 is configured in the central processing space S, and the reforming chamber heating flow chamber 7 is configured in the rightmost processing space S.
Then, in the processing space S constituting the reforming chamber 3, reforming of ruthenium, nickel, platinum, etc. for reforming the hydrocarbon-based raw fuel gas into a gas mainly composed of hydrogen gas using water vapor The reaction catalyst 19 is packed.

The reforming chamber 3 is configured such that raw fuel gas and water vapor are supplied from the upper end in a mixed state and flow downward, and the processing space S configured as the reforming chamber 3 and the above-mentioned At the lower end of the dish-shaped container forming member 51 that partitions the processing space S configured as the reforming chamber heating flow chamber 7, a fluid passage portion 54 that communicates the processing spaces S adjacent in the container alignment direction is provided. The reforming gas that has been reformed in the reforming chamber 3 is made 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 (that is, the outlet portion of the reforming process gas).

  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 to produce a reforming treatment gas mainly composed of hydrogen gas.

In addition, the reforming fuel is burned in the combustion chamber 6 at the lower end in the combustion chamber 6 constituted by the processing space S at the left end of the third container B3 from the left. A burner 17 is provided.
As shown in FIG. 4, the reforming burner 17 includes a first ejection pipe 17 </ b> A and a plurality of second ejection holes 17 b provided in a row by arranging a plurality of first ejection holes 17 a in the longitudinal direction. The second ejection pipes 17B arranged side by side are arranged side by side so that the ejection direction of the first ejection holes 17a and the ejection direction of the second ejection holes 17b intersect.
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.

At the time of startup in which the reforming burner 17 is ignited and the reforming chamber 3 is heated to a temperature capable of reforming, the same raw fuel gas as that supplied to the reforming chamber 3 is used as combustion fuel and combustion air. It is configured to be supplied to the first jet pipe 17A and burned in a mixed state, and during normal time when off-gas as exhaust fuel gas discharged from the fuel electrode of the fuel cell G is burned as combustion fuel, Off gas is supplied to the second jet pipe 17B, and combustion air is supplied to the first jet pipe 17A.
In addition, in order to heat the reforming chamber 3 so that the reforming process can be performed, when the off gas alone is insufficient, the raw fuel gas is mixed with the combustion air as the combustion fuel so as to compensate for the shortage. In this state, it is configured to be additionally supplied to the first jet pipe 17A.

The upstream heat exchange flow chamber 10 is configured in the left processing space S of the fourth container B4 (basic type container Bs) from the left, and the desulfurized raw fuel flow is configured in the right processing space S. A flow chamber 11 is configured, and the fourth vessel B4 from the left forms the heat exchanger Ea for raw fuel after desulfurization. In addition, as for container B4 which comprises this heat exchanger Ea for raw fuel after desulfurization, both of a pair of container formation members 51 are plate-shaped.
The starting electric heater 28 is provided in a state of being applied to the container forming member 51 on the right side of the fourth container B4 from the left constituting 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 space type container Bm having four processing spaces S in the container arrangement direction), the second processing space 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 processing space S from the left is a raw fuel flow chamber 13 before desulfurization. The rightmost processing space S is configured in the shift chamber 4 by being charged with an iron oxide-based or copper-zinc-based shift reaction catalyst 21 for converting carbon monoxide gas into carbon dioxide gas using water vapor. ing.
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.

  In addition, the dish-shaped container forming member 51 that partitions the leftmost processing space S and the second processing space S from the left, the second processing space S from the left and the third processing space S from the left. Each of the heat transfer plates 52 is provided with a fluid passage portion 54 communicating with the processing spaces S on both sides. Then, the desulfurization chamber 1 configured by the second processing space S from the left is the first stage, the desulfurization chamber 1 configured by the left end processing space 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 for desulfurization treatment.

Further, a dish-like container forming member 51 that partitions the third processing space S from the left that constitutes the raw fuel flow chamber 13 before desulfurization and the rightmost processing space 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 serve 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.
A start-up electric heater 29 for transformation processing is provided in a state of being applied to the auxiliary vessel forming member 53 that forms the transformation chamber 4 in the fifth vessel B5 from the left.

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

Further, a heat transfer plate 52 that partitions the second processing space S from the left and the third processing space S from the left, and a dish-shaped container that partitions the third processing space S from the left and the right processing space S Each of the forming members 51 is provided with a fluid passage portion 54 that communicates with the processing spaces S on both sides. Then, the transformation chamber 4 constituted by the second processing space S from the left is the second stage, the transformation chamber 4 constituted by the third processing space S from the left is the third stage, and the rightmost processing space. 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 caused to flow through the shift chambers 4 in the order of the second, third, and fourth stages to perform the shift process.
A shift temperature sensor Ts is provided so as to detect the temperature of the shift catalyst at the lower end portion of the fourth shift chamber 4 (that is, the outlet portion of the reforming process gas).
In addition, a starter electric heater 30 for the transformation process is provided in a state of being applied to the auxiliary container forming member 53 that forms the fourth stage of the transformation chamber 4 in the sixth container B6 from the left.

  Incidentally, in the shift chamber 4, carbon monoxide and water vapor in the reforming process 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. The modification reaction is carried out under the modification treatment temperature.

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

  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 space S of the container B is filled with a catalyst such as the reforming reaction catalyst 19 or the like, the flat container B is vertically oriented and slightly above the bottom of the processing space S. A porous catalyst receiving plate 55 is attached by welding to the container forming member 51, the heat transfer plate 52, or the dish-shaped auxiliary container forming member 53 that forms the processing space S in order to receive the catalyst at the portion. .

  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 A state in which the heat transfer coefficient setting 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 with each other, and configured to press the seven containers B in close contact from both sides in the container alignment direction while allowing relative movement in a direction perpendicular to the container alignment direction by the pressing means, Further, air is passed to the side of the rightmost container B7 constituting the selective oxidation chamber 5 toward the container B7. And a cooling fan 26 disposed so as, by its cooling fan 26, and is configured to cool the selective oxidation chamber 5. That is, the cooling fan 26 constitutes a cooling means for cooling 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 as to be able to transfer heat, and the desulfurization chamber 1, The conversion chamber 4 and the selective oxidation chamber 5 are arranged side by side from the reforming chamber 3 in the order of description, and adjacent ones are provided so as to be able to conduct heat, and the reforming chamber 3 and the combustion chamber 6 in the combustion chamber 6 are in close contact with each other. On the side, the evaporation treatment flow path 2 is provided so as to be able to conduct heat from the combustion chamber 6.

The operation control unit C adjusts the combustion amount of the reforming burner 17 so that the temperature of the reforming chamber 3 detected by the reforming temperature sensor Tr becomes the reforming set temperature, and The cooling amount is adjusted by adjusting the air flow rate of the cooling fan 26 so that the temperature of the selective oxidation chamber 5 detected by the selective oxidation temperature sensor Tm becomes the set temperature for selective oxidation. Yes.
Thus, the combustion amount of the reforming burner 17 is adjusted so that the temperature of the reforming chamber 3 becomes the reforming processing set temperature, and the temperature of the selective oxidation chamber 5 is set to the selective oxidation setting. The reforming chamber is in a state where the air flow rate of the cooling blower 26 is adjusted so as to reach a temperature, and in which the transformation chamber 4 is cooled by the combustion exhaust gas flowing through the cooling exhaust gas flow chamber 9. The temperature of each of the desulfurization chamber 1 and the shift chamber 4 located between 3 and the selective oxidation chamber 5 is a temperature at which the desulfurization process can be performed, a temperature at which the shift process can be performed, and the temperature at which the evaporation process flow path 2 can generate water vapor. Adjacent to each other, 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 combustion Each heat transfer coefficient between the chamber 6 and the evaporation treatment flow path 2 is set to a predetermined value.

  Hereinafter, the connection form of the flow path to each processing space S for supplying the fluid to each processing space S formed in each container B and discharging the fluid from each processing space S will be described. In each processing space 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 space S.

  A power generation raw fuel supply passage 31 is connected to the pre-desulfurization raw fuel flow chamber 13, and the second-stage desulfurization chamber 1 and the post-desulfurization raw fuel flow chamber 11 are connected to the post-desulfurization raw fuel flow chamber 11. And 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 chamber. The first-stage conversion chamber 4 that also serves as the flow-through chamber 12 is the first-stage conversion chamber 4 and the second-stage conversion chamber 4, and the fourth-stage conversion chamber 4 and the selective oxidation. Each of the chambers 5 is connected by a gas processing channel 32, and the selective oxidation chamber 5 and a fuel gas supply unit of the fuel cell G are connected by a fuel gas channel 33.

The power generation raw fuel supply path 31 includes a power generation raw fuel intermittent valve V1 for intermittently supplying the raw fuel gas for reforming, and a power generation for adjusting the supply amount of the raw fuel gas for reforming processing. A raw fuel control valve V2 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.

  In addition, a selective oxidation air supply passage 25 to which selective oxidation air is supplied from a selective oxidation blower 24 is provided in the gas processing flow passage 32 that connects the fourth stage shift chamber 4 and the selective oxidation chamber 5. The selective oxidation air is mixed with the reforming process gas that is connected and is subjected to the transformation treatment in the transformation chamber 4 and is 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 to the desulfurized raw fuel gas from the evaporation treatment flow path 2 to be described later through the water vapor flow path 34. Are mixed in the ejector 35, the raw fuel gas mixed with the water vapor is reformed in the reforming chamber 3, and the reformed gas is treated in the first, second, third, and fourth stages. In the shift chamber 4, the shift treatment gas is selectively oxidized in the selective oxidation chamber 5 to generate a hydrogen-containing gas having a low carbon monoxide concentration, and the hydrogen-containing gas is used as fuel. The gas is supplied to the fuel cell G through the fuel gas passage 33 as gas.

  The combustion chamber 6 and the heating exhaust gas flow chamber 8 are the heating exhaust gas flow chamber 8 and the cooling exhaust gas flow chamber 9, and the cooling exhaust gas flow chamber 9 and the economizer Ec The exhaust heat source exhaust gas flow chamber 14 is connected to each other by the combustion exhaust gas flow path 37, and the combustion exhaust gas discharged from the combustion chamber 6 is converted into a heating exhaust gas flow chamber 8, a cooling exhaust gas flow chamber 9, The exhaust heat source exhaust gas flow chamber 14 of the economizer Ec is configured to flow in order.

In an off gas passage 38 for leading off gas discharged from the fuel electrode of the fuel cell G as combustion fuel to be burned by the reforming burner 17, an off gas discharge portion of the fuel cell G and a combustion gas of the economizer Ec The flow chamber 15 is connected to the combustion gas flow chamber 15 and the second ejection pipe 17B of the reforming burner 17, respectively.
A bypass path 60 that bypasses the fuel cell G to connect the fuel gas path 33 and the off gas path 38 is provided, and the fuel cell G is connected to the fuel gas path 33 more than the connection point of the off gas path 38. Is provided with a fuel gas interrupting valve V5 for intermittently supplying fuel gas to the fuel cell G, and the bypass passage 60 is provided with a bypass opening / closing valve V6 for opening and closing the bypass passage 60, A battery downstream on-off valve V7 is provided at a location upstream of the connection location of the bypass passage 60 in the off-gas passage 38.

  A combustion blower 39 for supplying combustion air to the reformer burner 17 and the combustion air flow chamber 16 of the economizer Ec are connected to the combustion air flow chamber 16 and the reformer burner 17. One ejection pipe 17 </ b> A is connected by a combustion air flow path 40.

  Then, the economizer Ec recovers the exhaust heat of the combustion exhaust gas into off-gas and combustion air, pre-heats the off-gas and combustion air, and converts the pre-heated off-gas and combustion air into the reforming burner 17. It is comprised so that it may supply and burn to.

Further, a burner raw fuel supply passage 41 for supplying raw fuel gas as combustion fuel is connected to the first jet pipe 17A of the reforming burner 17.
The burner raw fuel supply passage 41 has a burner raw fuel intermittent valve V3 for intermittently supplying the raw fuel gas to the reforming burner 17, and the raw fuel gas supplied through the burner raw fuel supply passage 41. A burner raw fuel control valve V4 is provided for adjusting the supply amount of the burner.
The burner raw fuel supply passage 41 and the combustion air flow passage 40 are connected to the first jet pipe 17A in a state of being joined before the first jet pipe 17A, and burn the raw fuel gas. It is configured to be supplied to the first ejection pipe 17A in a state premixed with the working air.

  A reforming water supply channel 43 that supplies the reforming water in the reforming water tank 44 by the reforming water pump 42 is connected to the lower end of the evaporation processing channel 2, and is formed by the heating exhaust gas flow chamber 8. The water vapor channel 34 that guides the water vapor generated in the evaporation processing channel 2 by heating is connected to the ejector 35.

The first stage preheating heat exchanger 46 is provided so as to exchange heat between the reforming water flowing through the reforming water supply channel 43 and the fuel gas flowing through the fuel gas channel 33. The bypass path 60 is provided with a drain trap 48 for removing condensed water from the flowing gas.
The second stage preheating heat exchanger 47 includes the reforming water flowing through the reforming water supply channel 43 at a location downstream of the first stage preheating heat exchanger 46, and the fourth stage preheating heat exchanger 47. The reforming treatment gas flowing through the gas treatment flow path 32 connecting the shift chamber 4 and the selective oxidation chamber 5 is provided for heat exchange.
Further, a meandering channel portion 43d is provided at a location downstream of the second-stage preheating heat exchanger 47 in the reforming water supply channel 43, and the meandering channel portion 43d is 3 from the left. The container B3 is provided so as to be capable of conducting heat to the container forming member 51 that forms the combustion chamber 6 in the individual container B3, and flows through the reforming water supply passage 43 by conduction heat and radiation heat from the container forming member 51. The reforming water is preheated.
That is, the reforming water is preheated in the first-stage preheating heat exchanger 46, the second-stage preheating heat exchanger 47, and the meandering flow path portion 43d, and then is supplied to the evaporation processing flow path 2. It is configured to be supplied.

Further, in the gas processing flow path 32 connecting the fourth stage shift chamber 4 and the selective oxidation chamber 5, there is a waste heat recovery heat at a location downstream of the second stage preheating heat exchanger 37. An exchanger 49 is provided.
Although not shown, a hot water storage tank for storing hot water by heat generated from the fuel cell G is provided, and the fuel cell G is cooled by a heating heat exchanger provided in a hot water circulation path for circulating hot water in the hot water storage tank. The hot water in the hot water storage tank is heated by allowing the cooling water to flow therethrough.
The exhaust heat recovery heat exchanger 49 is provided in the hot water circulation path, recovers the exhaust heat of the reforming process gas flowing through the gas processing flow path 32, and supplies hot water flowing through the hot water circulation path. It is configured to heat.

Condensed water is removed from the reforming process gas at a location downstream of the exhaust heat recovery heat exchanger 49 in the gas processing flow path 32 connecting the fourth-stage shift chamber 4 and the selective oxidation chamber 5. A drain trap 50 is provided.
Condensed water removed by the drain trap 48 provided in the fuel gas flow path 33 is supplied to the reforming water tank 44 through a condensed water recovery path 61, and the fourth stage shift chamber 4 and the selective oxidation are supplied. The condensed water removed by the drain trap 50 provided in the gas processing flow path 32 connecting the chamber 5 is supplied to the reforming water tank 44 through the condensed water recovery path 62.
Although not shown, the condensed water obtained by condensing water vapor contained in the exhaust air discharged from the oxygen electrode of the fuel cell G or the combustion exhaust gas that has passed through the exhaust heat source exhaust gas flow chamber 14 of the economizer Ec. Condensed water obtained by condensing contained water vapor is also supplied to the reforming water tank 44.
That is, as described above, the condensed water recovered from the reforming gas, fuel gas, exhaust air, combustion exhaust gas, and the like is stored in the reforming water tank 44, and the stored condensed water is used as the reforming water. It is configured as follows.

Next, the control operation by the operation control unit C will be described.
In the normal operation in which the operation control unit C adjusts the generated power of the fuel cell G so as to follow the electric load, the detected temperature of the reforming temperature sensor Tr is set to the reforming processing set temperature. The burner raw fuel control valve V4 is adjusted to adjust the combustion amount of the reforming burner 17, and the combustion air is supplied to the reforming burner 17 in the amount of the combustion air that has a set air-fuel ratio. The reforming chamber temperature control for adjusting the rotational speed of the blower 39, the selective oxidation chamber temperature control for adjusting the rotational speed of the cooling blower 26 so that the detected temperature of the selective oxidation temperature sensor Tm becomes the set temperature for selective oxidation, The generated power adjustment control for controlling the power generation raw fuel control valve V2 to adjust the supply amount of the raw fuel gas so as to adjust the generated power of the fuel cell G according to the electric load, and S / C (raw Water vapor against fuel gas S / C adjustment control for controlling the rotational speed of the reforming water pump 42 so as to adjust the supply amount of the reforming water so that the target S / C becomes the target S / C. Execute.

Incidentally, the fuel utilization rate in the fuel cell G is set in advance, and the off-gas supplied to the reforming burner 17 based on the control information of the power generation raw fuel control valve V2 and the burner raw fuel control valve V4 The amount of combustion fuel combined with the raw fuel gas can be obtained.
Therefore, in the reforming chamber temperature control, the operation control unit C obtains the current amount of combustion fuel supplied to the reforming burner 17 (a total amount of off-gas and raw fuel gas) and obtains the obtained combustion. The rotational speed of the combustion blower 39 is adjusted so as to supply combustion air in an amount that is a set air-fuel ratio with respect to the supply amount of fuel.

  Incidentally, the set temperature for reforming treatment is set in a range of 600 to 750 ° C., for example, and the set temperature for selective oxidation is set in a range of 80 to 150 ° C., for example. The set air-fuel ratio is set to an air-fuel ratio that allows the reforming burner 17 to burn properly.

Then, the operation control unit C detects that the temperature of the shift chamber 4 detected by the shift temperature sensor Ts during normal operation (hereinafter may be referred to as a shift chamber temperature) from the set appropriate range for shift processing. If it becomes higher, the operation of the reforming water supply unit J is controlled so as to increase and adjust the supply amount of reforming water so as to increase the S / C (specifically, the rotation of the reforming water pump 42 is rotated). To adjust the speed).
Specifically, the operation control unit C, in the S / C adjustment control, when the shift chamber temperature detected by the shift temperature sensor Ts is within the set appropriate range, and the shift chamber temperature is lower than the set proper range. If the duration of the state higher than the set appropriate range is within the set time even if the value is higher, the target S / C is set to normal S / C and the shift chamber detected by the shift temperature sensor Ts When the duration time during which the temperature is higher than the set appropriate range exceeds the set time, the target S / C is set to the increase correction S / C, and the reforming water is set to the set target S / C. In order to adjust the supply amount, the rotational speed of the reforming water pump 42 is adjusted.
Incidentally, the set appropriate range is set to 150 to 400 ° C., for example, and the set time is set to about 1 minute, for example.
Further, the normal S / C is set to, for example, about 2.8 in the ratio of the amount of water vapor supply (number of moles) to the amount of raw fuel gas supplied to the reforming chamber 3 (number of moles of carbon). The correction S / C is set to be, for example, about 0.2 larger than the setting S / C.

Next, based on FIG.6 and FIG.7, the control action by the said operation control part C is demonstrated.
As shown in the flowchart of FIG. 6, at the start timing, the operation control unit C starts combustion of the reforming burner 17 and heats the reforming chamber 3 to a temperature at which reforming can be performed. A starting operation process for starting the reforming process of the raw fuel gas in the chamber 3 is executed, and when the starting operation process is completed, a normal operation process for adjusting the generated power of the fuel cell G so as to follow the electric load is performed. When it is executed and the stop timing is reached, the desulfurization chamber 1, the reforming chamber 3, the shift chamber 4, the selective oxidation chamber 5, and the gas processing flow path 32 connecting them are filled with raw fuel gas and hydrogen-containing gas A stop process for stopping the operation of the generator P is executed.
For example, when the fuel cell power generator is operated during a predetermined operation time zone 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.

A description will be given of the control operation in the startup operation process.
At the start timing, the fuel gas intermittent valve V5 and the battery downstream side open / close valve V7 are closed, and the bypass open / close valve V6 is opened, and the reforming chamber 3, The raw fuel gas filled in the shift chamber 4, the selective oxidation chamber 5, and the gas processing flow path 32 connecting them is set to the reforming burner 17, and then the operation of the combustion blower 39 is performed. And the burner raw fuel intermittent valve V3 is opened, and an igniter (not shown) is operated to start combustion of the reforming burner 17, and the auxiliary heating electric heater 27, The heating operation of the starter electric heaters 28, 29, and 30 is started.

Subsequently, when the reforming chamber temperature detected by the reforming temperature sensor Tr becomes equal to or higher than the reforming water supply start set temperature, the reforming water pump 42 starts to operate and enters the evaporation processing flow path 2. The supply of reforming water is started. Then, the water vapor generated in the evaporation processing flow path 2 is supplied to the reforming chamber 3, and the reforming chamber 3, the shift chamber 4, the selective oxidation chamber 5, and the gas processing flow path connecting them when stopped. 32 and the raw fuel gas filled in the fuel cell G and the fuel gas flow path 33 are pushed out by water vapor and supplied to the reforming burner 17.
Subsequently, when the reforming chamber temperature detected by the reforming temperature sensor Tr becomes equal to or higher than the raw fuel supply start set temperature, the power generation raw fuel intermittent valve V1 is opened to supply the desulfurization chamber 1 to the desulfurization chamber 1. The supply of the raw fuel gas is started, and the operation of the selective oxidation blower 29 is started to start the supply of the selective oxidation air.
Subsequently, when the set time for standby elapses, the fuel gas intermittent valve V5 and the battery downstream side open / close valve V7 are opened, and the bypass open / close valve V6 is closed to supply the fuel gas to the fuel cell G. Start supplying.
Thereafter, off-gas discharged from the fuel electrode of the fuel cell G is supplied to the reforming burner 17 as combustion fuel.

The reforming water supply starting set temperature is set to a temperature that can prevent thermal decomposition of raw fuel gas and condensation of water vapor, for example, 220 to 250 ° C., and the raw fuel starting set temperature is The temperature at which gas reforming can be performed, for example, 600 ° C. is set.
Further, the set time for standby is the start of the supply of the raw fuel gas to the desulfurization chamber 1, the reforming process in the reforming chamber 3, the shift process in the shift chamber 4, and the selective oxidation process in the selective oxidation chamber 5. Is set to the time required to stabilize.

Based on the flowchart shown in FIG. 7, the control operation of the normal operation process will be described.
The operation control unit C executes the above-described reforming chamber temperature control, selective oxidation chamber temperature control, and generated power adjustment control (steps # 1 to # 3), and then the conversion chamber detected by the conversion temperature sensor Ts. When the temperature is within the set appropriate range (step # 4) and when the transformation chamber temperature is higher than the set proper range and the duration of the state higher than the set proper range is within the set time (step #) 4, 5), the target S / C is set to the normal S / C (step # 6), and the duration of the state in which the shift chamber temperature detected by the shift temperature sensor Ts is higher than the set appropriate range is When the set time is exceeded (steps # 4 and 5), the target S / C is set to the increase correction S / C (step # 7), and the reforming water is supplied so as to be the set target S / C. Rotation of the reforming water pump 42 to adjust the amount Degrees modulate (step # 8).

The control operation in the stop process will be described.
At the stop timing, while the operation of the reforming water pump 42 is continued, the fuel gas intermittent valve V5 and the battery downstream side open / close valve V7 are kept open, and the bypass open / close valve V6 is opened. In addition, the power generation raw fuel intermittent valve V1 is closed to stop the supply of the raw fuel gas to the desulfurization section 1.
In this state, since the supply of the reforming water to the evaporation processing flow path 2 is continued, the water vapor generated in the evaporation processing flow path 2 is supplied to the reforming chamber 3 and the reforming chamber 3 The reforming chamber 4, the selective oxidation chamber 5, the reforming gas remaining in the gas processing channel 32 connecting them, and the fuel gas remaining in the fuel cell G and the fuel gas channel 33 are reformed. The fuel is supplied to the burner 17 and combusted, and the reforming chamber 3, the shift chamber 4, the selective oxidation chamber 5 and the gas processing channel 32 connecting them to each other, and the fuel cell G and the fuel gas channel 33 are filled with water vapor. .

Subsequently, when the reforming chamber temperature detected by the reforming temperature sensor Tr falls to the purge setting temperature, the operation of the reforming water pump 42 is stopped, and the power generation raw fuel intermittent valve V1 is turned on. By opening the valve, the raw fuel gas is supplied to the desulfurization chamber 1, the reforming chamber 3, the shift chamber 4, the selective oxidation chamber 5, the gas processing flow path 32 connecting them, the fuel cell G and the fuel The water vapor filled in the gas flow path 33 is discharged, the desulfurization chamber 1, the reforming chamber 3, the shift chamber 4, the selective oxidation chamber 5, the gas treatment flow channel 32 connecting them, the fuel cell G and the fuel When the raw fuel gas is filled in the gas flow path 33 and a preset purge setting time elapses, the bypass on-off valve V6 and the battery downstream side on-off valve V7 are closed, and then the power generation raw fuel intermittent valve V1 is closed, desulfurization chamber 1, reforming chamber 3, and transformation 4, the gas processing flow paths 32 for connecting the 5 and their selective oxidation chamber, and is filled with the raw fuel gas to the fuel cell G and the fuel gas flow path 33.
The purge set temperature is set to a temperature at which raw fuel gas can be prevented from thermal decomposition and water vapor can be prevented from condensing, for example, 400 ° C.

Hereinafter, based on FIG. 8, when the shift chamber temperature detected by the shift temperature sensor Ts becomes higher than the set appropriate range as described above, the shift chamber temperature can be lowered by increasing the S / C. The result of verifying that it can be explained.
In FIG. 8, the thin solid line indicates the change over time of the conversion chamber temperature detected by the conversion temperature sensor Ts, and the thick solid line indicates the change over time of S / C.
As shown in FIG. 8, it can be seen that when the S / C is increased from 2.8 to 3.0, the transformation chamber temperature can be lowered by about 20 ° C.

[Another embodiment]
Next, another embodiment will be described.
(A) When the transformation chamber temperature detected by the transformation temperature sensor Ts becomes higher than the appropriate setting range, the time during which the transformation chamber temperature is higher than the appropriate setting range becomes longer in increasing S / C. Alternatively, the value at which the S / C is increased and changed from the normal S / C may be increased as the transformation chamber temperature becomes higher than the appropriate setting range.

(B) 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.

(C) 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 The figure which shows the container which comprises a water vapor | steam production | generation part. 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 Diagram explaining the result of verification test

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Desulfurization part 3 Reforming part 4 Transformation part 5 Selective oxidation part 9 Heat exchange part 17 for heat recovery Combustion heating means 26 Cooling means C Operation control means J Water supply means for reforming

Claims (2)

A reforming section for reforming a hydrocarbon-based raw fuel to generate a reformed gas containing hydrogen gas as a main component;
A transformation section that transforms carbon monoxide gas in the reforming gas supplied from the reforming section into carbon dioxide gas and is cooled in a heat exchange section for heat recovery;
Combustion-type heating means for heating the reforming part so as to allow a reforming process and heating the metamorphic part so as to allow a modification process;
Reforming water supply means for supplying reforming water for reforming raw fuel in the reforming section;
A hydrogen-containing gas generation device provided with an operation control means for controlling operation,
The operation control means controls the operation of the heating means so that the temperature of the reforming section falls within a proper setting range for reforming treatment, and the temperature of the metamorphic section is lower than the proper setting range for transformation processing. Is higher, the operation of the reforming water supply means is controlled to increase and adjust the supply amount of reforming water so as to increase the steam / carbon ratio, which is the ratio of the amount of steam to the raw fuel. A hydrogen-containing gas generator. The reforming unit, a desulfurization unit that desulfurizes the raw fuel supplied to the reforming unit, the shift unit, and a carbon monoxide gas in the reforming process gas supplied from the shift unit are selectively oxidized. A selective oxidation unit is provided between the reforming unit and the selective oxidation unit so that the desulfurization unit and the transformation unit are located, and adjacent ones can conduct heat,
The heating means is provided adjacent to the side of the reforming unit opposite to the side where the desulfurization unit and the transformation unit are provided so as to heat the reforming unit,
A cooling means for cooling the selective oxidation unit is provided;
The operation control unit adjusts the heating amount of the heating unit so that the temperature of the reforming unit becomes the preset temperature for reforming process, and the temperature of the selective oxidation unit becomes the preset temperature for selective oxidation. The hydrogen-containing gas generating device according to claim 1, wherein the cooling amount of the cooling means is adjusted to the above.

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