JP2007290901A - Heat exchange type reformer - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a heat exchange type reformer which is good in the heat exchange efficiency between a heating part and a reforming part. <P>SOLUTION: In the heat exchange type reformer 10, a reforming flow passage 18, on which a reforming catalyst for a reforming reaction is supported, and a combustion flow passage 20, on which an oxidation catalyst for combustion is supported, are adjacent to each other through a plate part 52. In the reforming flow passage 18 for forming a hydrogen-containing reformed gas from a supplied reforming raw material and the combustion flow passage 20 for supplying heat generated by the catalytic combustion of a supplied fuel to the reforming flow passage 18, the gas flow directions are both set to be in the direction as indicated by the arrow F, and thereby, a parallel-flow type heat exchanger is constituted in heat exchange flow passages 58A, 64A. At the upstream in the gas flow direction of the heat exchange flow passages 58A, 64A, a reforming gas guide flow passage 58B for guiding the reforming raw material to the heat exchange flow passage 58A along a predetermined direction and a mixed gas guide flow passage 64B for guiding the fuel to the heat exchange flow passage 64A along the direction crossing with the gas flow direction in the reforming gas guide flow passage 58B are provided. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a heat exchange type reformer that performs a reforming reaction for obtaining a reformed gas containing hydrogen from a reforming raw material such as a hydrocarbon while receiving heat supply from a heating unit in the reforming unit.

A reforming channel for reforming a hydrocarbon raw material to generate a hydrogen-containing gas between a plurality of stacked plates, and a fuel gas for supplying heat for reforming reaction to the reforming channel A cross flow heat exchange type fuel reformer having a combustion flow path for combustion is known (see, for example, Patent Document 1). Patent Document 1 describes a technique for setting a non-supported region of a catalyst between plates so that an exothermic distribution of a combustion reaction and an endothermic distribution of a reforming reaction at each part between the plates are adjusted.
Japanese Patent Application Laid-Open No. 2004-244230

  In the conventional cross-flow heat exchange type fuel reformer described above, a device has been devised to make the high heat generation part due to the combustion reaction coincide with the high heat absorption part due to the reforming reaction. There was room for improvement in terms of improving exchange efficiency.

  In view of the above facts, an object of the present invention is to obtain a heat exchange type reformer having good heat exchange efficiency between the heating section and the reforming section.

  In order to achieve the above object, a heat exchange type reformer according to the invention described in claim 1 carries a reforming catalyst for reforming reaction and is supplied by a reforming reaction including a steam reforming reaction. A reforming section for generating reformed gas containing hydrogen from the raw material, and adjacent to the reforming section via a partition so as to generate a gas flow in the same direction as the gas flow of the reforming section; An oxidation catalyst for catalytic combustion is carried, a heating unit for supplying heat generated by catalytic combustion of the supplied fuel to the reforming unit, and one end side serving as a supply port for the reforming raw material The reformed raw material introduction part is connected to the reforming raw material inflow side in the reforming part, and the other end is connected to the fuel inflow side in the heating part. However, it is different from the flow direction of the reforming material by the reforming material introducing section. Re includes a fuel inlet portion for guiding the fuel to the heating unit in the direction.

  In the heat exchange type reformer according to claim 1, while the reforming unit receives heat supply from the heating unit through combustion, the supplied reformed gas is brought into contact with the reforming catalyst to cause a reforming reaction (acceleration). And a reformed gas containing hydrogen is obtained. The reforming reaction generates a high endothermic site in the vicinity of the upstream end (reforming raw material supply side) in the reforming catalyst support range, and the combustion reaction is the upstream side (fuel supply side) in the oxidation catalyst support range. A highly exothermic part is generated in the vicinity of the end of the plate.

  Here, since the flow direction of the reforming raw material (reformed gas) in the reforming section and the flow direction of the fuel or combustion gas in the heating section are the same, in other words, in the heating section and the reforming section. Since a parallel flow heat exchange type reformer is configured, a high heat generation site due to a combustion reaction in the heating unit and a high heat absorption site due to the reforming reaction in the reforming unit are arranged in the direction of gas flow in each catalyst support range. It can occur on the same side (upstream side). That is, it is possible to bring a portion where heat generation is large close to a portion where the endothermic demand is large (matching the distribution tendency of heat absorption and heat generation).

  And in this heat exchange type | mold reformer, the reforming raw material introducing | transducing part continuous in the upstream end of a reforming part and the reforming part are made into a parallel flow (medium inlet as a heat exchanger is made to correspond substantially). Since the fuel introduction section that is continuous with the upstream end of the heating section is configured to cause the flow of the medium in different directions, in other words, in a pseudo manner between the reforming raw material introduction section and the fuel introduction section. Since the cross flow portion is configured, the reforming material supply port and the fuel supply port can be opened independently. As a result, the reforming raw material and fuel can be supplied independently to the same side of the reforming section and the heating section. An exchange type reformer can be constructed.

  Thus, in the heat exchange type | mold reformer of Claim 1, the heat exchange efficiency of a heating part and a reforming part is favorable. In addition, since heat exchange between the reformed raw material flowing through the reformed raw material introduction section and the fuel flowing through the fuel introduction section is performed, operational stability (robustness) is improved and fluctuations (for example, temperature change of the reformed raw material). In contrast, stable operation is possible.

  A heat exchange type reformer according to a second aspect of the present invention is the heat exchange type reformer according to the first aspect, wherein the entire fuel introduction part is a non-supporting region of the oxidation catalyst.

  In the heat exchange type reformer of the second aspect, since the oxidation catalyst is not supported on the fuel introduction part, catalytic combustion does not occur in the fuel introduction part. Thereby, it is prevented that the heat generated by the catalytic combustion is not consumed by the reforming unit and a local high-temperature part is generated. In particular, even in the configuration in which the reforming catalyst is supported on the reforming raw material introduction part, when the oxidation catalyst is supported on the fuel introduction part that forms the above-described pseudo cross flow part with the reforming raw material introduction part, the high Although a local high temperature part may be generated due to a mismatch between the heat generation part and the high heat absorption part, the local high temperature part is effectively prevented by not supporting the oxidation catalyst in the fuel introduction part.

  A heat exchange type reformer according to a third aspect of the present invention is the heat exchange type reformer according to the first or second aspect, wherein a plurality of the reforming sections and heating sections are provided. The reforming raw material introduction section is provided in each layer of the reforming section to match the opening surface of the reforming raw material supply port, and the fuel introduction section is Provided in each layer of the heating unit, the opening surfaces of the fuel supply ports are matched.

  In the heat exchange type reformer according to claim 3, at least a part of the reforming unit and the heating unit are adjacent to each other by stacking the plurality of reforming units and the heating unit. In addition, it is preferable that the heating unit is provided in the same number or fewer than the reforming unit, and all of them are adjacent to the reforming unit on both sides in the stacking direction. Here, a reforming raw material introduction portion that opens at an opening surface that matches each reforming portion of each layer is provided, and a fuel introduction portion that opens at an opening surface that matches each heating portion of each layer is provided, The reforming raw material and fuel can be supplied independently to the same side of each reforming unit and heating unit, and as described above, a parallel flow type heat exchange type in which a part with large heat generation is brought close to a part with large heat absorption requirements A reformer can be comprised by the laminated structure with favorable heat exchange efficiency.

  A heat exchange type reformer according to a fourth aspect of the present invention is the heat exchange type reformer according to the third aspect, wherein the reformer is formed between a flat plate portion formed in a flat plate shape and another flat plate portion. The reforming material is provided between the heat exchanging portion that constitutes a portion and a standing wall that guides the reforming material in a predetermined direction on the supply side of the reforming material with respect to the heat exchanging portion. The reforming part forming plate member in which the reforming material guide part constituting the introduction part is formed, and the flat plate part formed in a flat plate shape, and the other side of the flat plate portion is loaded with the oxidation catalyst. And a standing wall for guiding the fuel in a direction intersecting a predetermined direction of the reforming portion forming plate member on the fuel supply side with respect to the heat exchange portion. A fuel guide portion which is erected and constitutes the fuel introduction portion between the other flat plate portion and It is constructed by laminating a heating unit forming plate member that is made, in a predetermined pattern.

  5. The heat exchange type reformer according to claim 4, wherein the reforming section forming plate member and the heating section forming plate member are laminated in a predetermined pattern, so that the reforming section is provided between the heat exchange sections of each flat plate section. A heating part is formed, and a reforming material introduction part and a fuel introduction part are formed between the reforming material guide part and the fuel guide part of each flat plate part. That is, a reforming material supply port that opens independently on the upstream side of the parallel flow type heat exchange unit by laminating the reforming unit forming plate member and the heating unit forming plate member in a predetermined pattern. The reforming raw material introduction unit having the fuel supply port and the fuel introduction unit are integrally configured.

  A heat exchange type reformer according to a fifth aspect of the present invention is the heat exchange type reformer according to the third or fourth aspect, wherein the reforming raw material supply ports of the plural reforming raw material introduction sections are open. And a reforming material manifold for distributing and supplying the reforming materials to the plurality of reforming material introduction portions, and a gathering space in which the fuel supply ports of the plurality of fuel introduction portions are opened. And a manifold for fuel for supplying fuel to the plurality of fuel introduction portions in a distributed manner.

  In the heat exchange type reformer according to claim 5, each supply port of the reforming material introduction section for introducing the reforming material into the reforming section of each layer is opened by a manifold for reforming material, and heating of each layer is performed. Each supply port of the fuel introduction part for introducing fuel into the part is opened by a fuel manifold. For this reason, the reforming material can be evenly distributed from the reforming material manifold to the reforming part of each layer via the reforming material introduction part of each layer, and similarly, the fuel introduction part of each layer from the fuel manifold. It becomes possible to distribute fuel evenly to the heating parts of the respective layers via the. In particular, by providing a fuel manifold with a mixer of fuel and supporting gas, it is possible to supply the mixed gas premixed immediately upstream of the heating section of each layer to the heating section of each layer. In this case, a portion having a high fuel concentration is prevented from being locally generated, and a local high temperature portion is prevented from being generated in the heating portion.

  A heat exchange type reformer according to a sixth aspect of the present invention is the heat exchange type reformer according to any one of the first to fifth aspects, wherein one end side is an outlet for the reformed gas. And the other end side is a reformed gas outlet portion continuous to the reformed gas outflow side in the reforming portion, and one end side is a combustion exhaust gas discharge port of the heating portion, and the other end side is the combustion in the heating portion. A combustion exhaust gas discharge unit that is continuous with the exhaust gas discharge side and guides the combustion exhaust gas to the combustion exhaust gas discharge port in a flow direction different from a flow direction of the reformed gas by the reformed gas deriving unit;

  In the heat exchange type reformer according to claim 6, the reformed gas lead-out section continuous to the downstream end of the reforming section and a parallel flow with the reforming section (with the medium outlet as the heat exchanger being substantially coincident with each other) In other words, the combustion exhaust gas discharge section that is continuous with the downstream end of the heating section is configured to generate a medium flow in different directions. In other words, the reformed gas discharge section and the combustion exhaust gas discharge section Therefore, the reformed gas discharge port and the combustion exhaust gas discharge port can be opened independently. As a result, the reformed gas and the combustion exhaust gas can be discharged independently from the same side of the reforming unit and the heating unit. A heat exchange type reformer can be constructed.

  In a configuration in which a plurality of reforming units and a plurality of heating units are stacked so that at least a part of the reforming units and the heating unit are adjacent to each other, a reforming gas deriving unit is provided in the reforming unit of each layer. It is preferable to provide a combustion exhaust gas discharge part in the heating part of each layer. In particular, in the configuration in which the reforming part forming plate member and the heating part forming plate member are laminated in a predetermined pattern, the heat exchange part in the flat plate part of the reforming part forming plate member is opposite to the reforming material guide part. On the side, a standing wall for separately guiding the reformed gas in a predetermined direction is erected, and a reformed gas guide portion constituting a reformed gas lead-out portion is formed between the other flat plate portion, and a heating portion forming plate On the opposite side of the heat exchanging portion of the flat plate portion of the member from the fuel guide portion, another flat plate portion is provided with a standing wall for guiding the combustion exhaust gas in a direction crossing a predetermined direction of the reforming portion forming plate member. It is preferable that the exhaust gas guide part constituting the fuel introduction part is formed between the two. In this configuration, by laminating the reforming part forming plate member and the heating part forming plate member in a predetermined pattern, the inlets and outlets of the respective media with respect to the parallel flow type heat exchanger can be provided independently.

  As described above, the heat exchange type reformer according to the present invention has good heat exchange efficiency between the heating section and the reforming section.

  A heat exchange type reformer 10 according to a first embodiment of the present invention will be described with reference to FIGS. 1 to 6. First, the overall system configuration of the fuel cell system 11 to which the heat exchange reformer 10 is applied will be described, and then the detailed structure of the heat exchange reformer 10 will be described.

(Overall configuration of fuel cell system)
FIG. 4 shows a system configuration diagram (process flow sheet) of the fuel cell system 11. As shown in this figure, the fuel cell system 11 includes a fuel cell 12 that generates power by consuming hydrogen, and a heat exchange reforming process for generating hydrogen-containing reformed gas to be supplied to the fuel cell 12. The reactor (reformer) 10 is a main component.

  The fuel cell 12 is configured by sandwiching an electrolyte (not shown) between an anode electrode (fuel electrode) 14 and a cathode electrode (air electrode) 16. The fuel cell 12 mainly includes hydrogen supplied to the anode electrode and the cathode electrode 16. It is configured to generate electricity by electrochemical reaction with supplied oxygen. Although various types of fuel cells 12 can be employed, in this embodiment, the fuel cell 12 is operated in an intermediate temperature range (about 300 ° C. to 600 ° C.) and water is generated at the cathode electrode 16 along with power generation. A fuel cell (for example, a solid polymer type or a hydrogen separation membrane type fuel cell) having a produced proton-conducting electrolyte is employed.

  As shown in FIG. 4, the heat exchange type reformer 10 includes a reforming flow path 18 as a reforming section that generates a hydrogen-containing reformed gas to be supplied to the anode electrode 14 of the fuel cell 12, and a reformer. The mass flow path 18 includes a combustion flow path 20 as a heating unit for supplying heat for performing the reforming reaction. A reforming catalyst 22 is supported in the reforming channel 18, and hydrogen gas is produced by catalytic reaction of the supplied hydrocarbon gas (gasoline, methanol, natural gas, etc.) and reforming gas (steam). Is generated (reforming reaction is performed).

The reforming reaction in the reforming channel 18 includes each reaction including the steam reforming reaction represented by the formula (1) as represented by the following formulas (1) to (4). Therefore, the reformed gas obtained in the reforming process includes hydrogen (H ₂ ), carbon monoxide (CO), methane (CH ₄ ), cracked hydrocarbons, unreacted raw material hydrocarbons (C _x H _y ), etc. Combustible gas and carbon dioxide (CO ₂ ), water (H ₂ O), and other non-flammable gases.

_{C n H m + nH 2 O} → nCO + (n + m / 2) H 2 ... (1)
_{C n H m + n / 2O} 2 → nCO + m / 2H 2 ... (2)
CO + H ₂ O⇔CO ₂ + H ₂ (3)
CO + 3H ₂ ＣＨCH ₄ + H ₂ O (4)
The main steam reforming reaction of the formula (1) in the reforming reaction is an endothermic reaction, and the reforming channel 18 is supplied to the fuel cell 12 operated at an intermediate temperature or a high temperature as described above. Is supplied at a temperature higher than a predetermined temperature. The combustion channel 20 is configured to supply heat for maintaining the reforming reaction and operating temperature in the reforming channel 18. The combustion flow path 20 is provided adjacent to the reforming flow path 18 carrying the oxidation catalyst 24, and is configured to cause catalytic combustion by bringing the supplied fuel into contact with the oxidation catalyst 24 together with oxygen. . Further, the partial oxidation reaction of the formula (2) is an exothermic reaction, and the heat generated by this partial oxidation reaction is used for the steam reforming reaction together with the heat from the combustion channel 20.

  The heat exchange reformer 10 supplies combustion heat obtained by catalytic combustion of fuel in the combustion channel 20 to the reforming channel 18 via a plate portion 52 described later. For this reason, the amount of heat is directly applied to the reforming channel 18 without converting the amount of heat into temperature as in the configuration in which the reforming channel 18 is heated via a heat medium (fluid) such as combustion gas. It can be configured.

  The fuel cell system 11 includes a raw material pump 26 for supplying a hydrocarbon raw material to the reforming flow path 18, and a discharge portion of the raw material pump 26 is connected to the reforming flow path 18 via a raw material supply line 28. It is connected to the raw material inlet 18A. The hydrocarbon raw material slightly contains a sulfur component (sulfur compound) that does not contribute to the above reforming reaction. This hydrocarbon raw material is supplied to the reforming flow path 18 in a gas phase or atomized state, for example, by a vaporizing means (not shown) such as an evaporator or an injection.

  The reformed gas outlet 18 </ b> B of the reforming channel 18 is connected to the upstream end of the reformed gas supply line 30 whose downstream end is connected to the fuel inlet 14 </ b> A of the anode electrode 14. Thereby, the reformed gas generated in the reforming channel 18 is supplied to the anode electrode 14 of the fuel cell 12. On the other hand, the upstream end of the anode offgas line 32 is connected to the offgas outlet 14B of the anode electrode 14, and the downstream end of the anode offgas line 32 is connected to the fuel inlet 33A of the gas mixer 33. The gas mixer 33 is configured to substantially uniformly mix a cooling off gas and an anode off gas supplied from a support gas supply line 46 described later. A mixed gas outlet 33 </ b> B of the gas mixer 33 is connected to a fuel (mixed gas) inlet 20 </ b> A of the combustion flow path 20.

As described above, in the fuel cell system 11, the hydrogen in the reformed gas generated in the reforming channel 18 is consumed in the fuel cell 12, and the remaining components other than the consumed hydrogen are supplied to the combustion channel 20 as anode offgas. Combustible components (hydrogen (H ₂ ), carbon monoxide (CO), hydrocarbon (HC), methane (CH ₄ ), carbon dioxide (CO ₂ )) are consumed as fuel in the combustion channel 20. It has become so. An exhaust gas line 34 for discharging combustion exhaust gas to the outside of the system is connected to the exhaust gas outlet 20B of the combustion flow path 20.

  The fuel cell system 11 also includes a cathode air pump 36 for supplying cathode air to the cathode electrode 16, and the discharge portion of the cathode air pump 36 has an air inlet 16 </ b> A at the downstream end of the cathode electrode 16. The upstream end of the cathode air supply line 38 connected to is connected. Further, the upstream end of the steam supply line 40 is connected to the off-gas outlet 16B of the cathode electrode 16, and the downstream end of the steam supply line 40 is connected to the steam inlet 18C of the reforming flow path 18. As a result, the cathode off gas containing water vapor generated at the cathode electrode 16 and oxygen not consumed at the cathode electrode 16 is supplied to the reforming channel 18. Then, water vapor in the cathode off-gas is used for the steam reforming reaction of the formula (1), and oxygen is used for the partial oxidation reaction of the formula (2). That is, the heat exchange type reformer 10 according to the present embodiment supplies the cathode offgas containing oxygen to the reforming flow path 18, so that the ratio of the supplied oxygen amount to the carbon amount in the hydrocarbon weight loss is O /. The C ratio is configured to be operated under a specific condition.

  Further, the fuel cell system 11 includes a cooling air pump 42 for supplying cooling air to the fuel cell 12, and the discharge part of the cooling air pump 42 has a refrigerant flow path ( It is connected to the upstream end of the cooling air line 44 connected to the inlet 12A (not shown). The refrigerant flow path outlet 12 </ b> B is connected to the upstream end of the combustion support gas supply line 46. The combustion support gas supply line 46 is connected to the support gas inlet 33C of the gas mixer 33, and supplies a cooling off gas containing oxygen as a combustion support gas to the gas mixer 33. Thereby, in the combustion flow path 20, the anode off gas from the anode off gas line 32 and the cooling off gas from the combustion support gas supply line 46 are brought into contact with the oxidation catalyst 24 containing the mixed gas mixed in the gas mixer 33. Thus, it is configured to cause catalytic combustion.

  In the fuel cell system 11, for example, a separation membrane (a porous material separation membrane such as polyimide or ceramic) that selectively transmits only water vapor in the cathode offgas is provided in the water vapor supply line 40, or reforming water vapor is supplied. By introducing it from outside the system, a configuration in which oxygen is not supplied to the reforming flow path 18 or a configuration in which the amount of oxygen supplied (O / C ratio) to carbon in the hydrocarbon raw material is reduced can be achieved. In these configurations, the main reaction of the reforming reaction in the heat exchange reformer 10 is a steam reforming reaction, and the partial oxidation reaction is not performed or the heat generation amount due to the partial oxidation reaction becomes extremely small.

(Configuration of heat exchange type reformer)
FIG. 1 shows an exploded perspective view of the laminated core portion 65 of the heat exchange type reformer 10. As shown in this figure, the heat exchange type reformer 10 includes a plurality of stacked reforming portion forming plate members and unit plate members 50 and 51 as heating portion forming plate members as reforming portions. The reforming flow path 18 and the combustion flow path 20 as a heating part are formed as independent gas flow paths separated by a plate part 52 as a flat plate part of the unit plate members 50 and 51 as a partition wall. In this embodiment, the reforming flow path 18 and the combustion flow path 20 are alternately arranged in the stacking direction (thickness direction of the plate portion 52), and are adjacent to each other via the plate portion 52. This will be specifically described below.

  The unit plate member 50 includes a plate portion 52 formed in a flat plate shape. The plate part 52 is configured such that flow direction conversion parts 52B and 52C are continuously provided on both sides in the longitudinal direction of a parallel flow part 52A serving as a rectangular heat exchange part in a plan view. In this embodiment, the flow direction conversion parts 52B and 52C are each formed in a triangular shape such that the bottom side coincides with the short side of the parallel flow part 52A (rectangular shape). It is formed into a shape. Each unit plate member 50 includes an outer wall 54 erected from the periphery of the plate portion 52 on the side where the reforming flow path 18 is formed.

  The outer wall 54 is a spacer that forms the reforming flow path 18 between the stacked unit plate members 50 and 51 by being erected from the entire circumference of the plate portion 52 except for each side portion of the direction changing portions 52B and 52C. In addition to fulfilling the function and the outer wall function of preventing gas outflow from the reforming flow path 18, the gas inlet 50A on the flow direction changing portion 52B side and the gas outlet 50B on the flow direction changing portion 52C side are formed. The gas inlet 50A and the gas outlet 50B are formed symmetrically with respect to the centroid of the plate part 52, and are opposite to the parallel flow part 52A along the longitudinal direction of the outer wall 54 in the flow direction conversion parts 52B and 52C, respectively. Opening is directed in the direction of arrow C1 and arrow C2.

  A plurality of standing walls (partition walls) 56 that divide the reforming channel 18 into a plurality of parallel channels are provided upright from the side of the plate portion 52 of the unit plate member 50 where the reforming channel 18 is formed. Each standing wall 56 is substantially parallel to the outer wall 54 from the gas inlet 50 </ b> A to the gas outlet 50 </ b> B, and is configured to partition the reforming channel 18 into a plurality of divided channels (microchannels) 58. Each divided flow path 58 is formed in a crank shape in which the flow path length from the gas inlet 50A to the gas outlet 50B is substantially constant by the symmetrical arrangement of the gas inlet 50A and the gas outlet 50B.

  And in the parallel flow part 52A in each division | segmentation flow path 58, the part divided by the partition part 56A of each standing wall 56 along the longitudinal direction of this parallel flow part 52A is set as the heat exchange flow path 58A, respectively. On the other hand, the portion where the inlet guide wall 56B along the direction of the arrow C1 among the standing walls 56 is erected from the flow direction conversion portion 52B in each divided flow channel 58 is a reforming material guide flow channel 58B as a reforming material guide portion. It is said that. Further, the portion of each standing channel 56 where the outlet guide wall 56C is provided in the direction of the arrow C2 from the flow direction changing portion 52C in each divided channel 58 is a reformed gas guide channel 58C as a reformed gas guide unit. It is said that.

  The unit plate member 51 includes a plate portion 52 having the same shape as the plate portion 52 constituting the unit plate member 50, and an outer wall 60 standing on the formation side of the combustion flow path 20 from the periphery of the plate portion 52. I have. The outer wall 60 is erected from the entire circumference of the plate portion 52 except for each one side portion in the direction changing portions 52B and 52C, thereby forming a combustion channel 20 between the stacked unit plate members 51 and 50. In addition to fulfilling the outer wall function of preventing gas outflow from the combustion flow path 20, a gas inlet 51A on the flow direction changing portion 52B side and a gas outlet 51B on the flow direction changing portion 52C side are formed.

  The gas inlet 51A is different from the direction of the arrow C1 in which the gas inlet 50A opens on the same side in the longitudinal direction as the gas inlet 50A of the unit plate member 50 (arrow A side in FIG. 1) with respect to the parallel flow portion 52A (parallel flow). It is formed so as to open in the direction of the arrow D1 (symmetric to the longitudinal direction of the portion 52A). Further, the gas outlet 51B is different from the direction of the arrow C2 in which the gas outlet 50B is opened on the same side of the parallel outlet 52A as the gas outlet 50B of the unit plate member 50 in the longitudinal direction (arrow B side in FIG. 1) ( It is formed so as to open in the direction of the arrow D2 (symmetric with respect to the longitudinal direction of the parallel flow portion 52A).

  A plurality of standing walls (partition walls) 62 that divide the combustion channel 20 into a plurality of parallel channels are provided upright from the side of the plate portion 52 of the unit plate member 51 where the reforming channel 18 is formed. Each standing wall 62 is substantially parallel to the outer wall 60 from the gas inlet 51 </ b> A to the gas outlet 51 </ b> B, and is configured to partition the combustion channel 20 into a plurality of divided channels (microchannels) 64. Each divided flow path 64 is formed in a crank shape in which the flow path length from the gas inlet 51A to the gas outlet 51B is substantially constant due to the symmetrical arrangement of the gas inlet 51A and the gas outlet 51B.

  And in the parallel flow part 52A in each division | segmentation flow path 64, the part divided by the partition part 62A of each standing wall 56 along the longitudinal direction of this parallel flow part 52A is set as the heat exchange flow path 64A, respectively. On the other hand, the portion of each standing wall 62 where the inlet guide wall 62B is erected along the direction of the arrow D1 from the flow direction conversion section 52B in each divided flow path 64 is a mixed gas guide flow path 64B as a fuel guide section. Yes. Furthermore, the part where the outlet guide wall 62C along the direction of the arrow D2 among the standing walls 62 is erected from the flow direction conversion part 52C in each divided flow path 64 is a combustion exhaust gas guide flow path 64C as a combustion exhaust gas guide part. ing.

  In the heat exchange type reformer 10 described above, the gas inlets 50A and 51A are located on the same side (arrow A side) with respect to the parallel flow part 52A (heat exchange flow paths 58A and 64A) as described above, and the gas outlet 50B. , 51B are located on the same side (arrow B side) with respect to the parallel flow portion 52A, the gas flow directions in the heat exchange flow path 58A and the heat exchange flow path 64A of each layer are the same direction (arrow F direction). ing.

  The unit plate member 50 and the unit plate member 51 described above are made of, for example, a metal material such as stainless steel or a solid (not porous) ceramic material, and each part (plate portion 52, outer wall 54, standing wall 56, Alternatively, the plate portion 52, the outer wall 60, and the standing wall 62) are integrally formed. Further, each of the plurality of unit plate members 50 and the unit plate members 51 is laminated, and the plate portion 52 and the outer wall 54 or the outer wall 60 (respective standing walls 56 and 62) are brazed or diffused using, for example, a brazing material. The laminated core portion 65 of the heat exchange reformer 10 is configured to be airtightly joined by joining. As shown in FIG. 2, in this embodiment, the heat exchange type reformer 10 is reformed by laminating a flat plate portion 52 (cover) on which the outer wall 54 or the like is not erected on the top. The flow path 18 is closed.

  As shown in FIG. 2, the laminated core portion 65 is connected to a reforming inlet manifold 66 that forms a collective space in which gas inlets 50 </ b> A of the respective layers are opened. Also, the laminated core portion 65 is connected to a reforming outlet manifold 68 that forms a collective space in which the gas outlets 50B of the respective layers are opened. Further, a combustion inlet manifold 70 that forms a collective space in which the gas inlet 51A of each layer opens is connected to the laminated core portion 65. Furthermore, the laminated core portion 65 is connected to a combustion outlet manifold 72 that forms a collective space in which the gas outlets 51B of the respective layers are opened. Each manifold 66, 68, 70, 72 is formed in a rectangular cylinder shape, and one open end is joined to the uppermost lower plate portion 52 and the outer wall 54 of each layer, and the end of the outer wall 60 by brazing or the like. Yes.

  The reforming inlet manifold 66 is provided with a raw material inlet 18A and a steam inlet 18C for introducing a reforming raw material (hydrocarbon) and steam (cathode off-gas), and the reforming outlet manifold 68 has a reformed gas. Is provided with a reformed gas outlet 18B. The combustion inlet manifold 70 is provided with a fuel inlet 20A for introducing the mixed gas from the gas mixer 33, and the combustion outlet manifold 72 is provided with an exhaust gas outlet 20B for discharging combustion exhaust gas. It has been.

  In the heat exchange type reformer 10 (laminated core portion 65) described above, the reforming catalyst 22 is carried on the inner surface of the divided flow path 58 in the unit plate member 50, and the divided flow path in the unit plate member 51. An oxidation catalyst 24 is supported on the inner surface of 64. As shown in FIG. 3 which is an exploded plan view in which the standing walls 56 and 62 are not shown, the reforming catalyst 22 is a predetermined excluding a part of the divided channel 58 (reforming channel 18) on the gas inlet 50A side. The oxidation catalyst 24 is supported over a predetermined range excluding a part of the divided flow path 64 (combustion flow path 20) on the gas inlet 51A side.

  More specifically, as shown in FIG. 3, the reforming catalyst 22 includes upstream support ends 22 </ b> A that are upstream (arrow A side) ends in the gas flow direction to which the reforming raw material is supplied. This substantially coincides with the boundary between the heat exchange channel 58A (parallel flow part 52A) and the reformed gas guide channel 58B (flow direction changing part 52B) in the divided channel 58. On the other hand, in the oxidation catalyst 24, the upstream carrying end 24A, which is the upstream end (arrow A side) in the gas flow direction to which fuel is supplied, has a heat exchange flow path 64A (parallel flow section) in each divided flow path 64. 52A) and the mixed gas guide channel 64B (flow direction changing portion 52B) substantially coincide with each other. The upstream carrying end 24A of the oxidation catalyst 24 coincides with the upstream carrying end 22A of the reforming catalyst 22 or is located slightly downstream from the upstream carrying end 22A.

  In the heat exchange type reformer 10, as shown in FIGS. 5A and 5B, the laminated core portion 65 is stored in the gas outlet 50B, and the storage tank 76 storing the slurry-like catalyst carrier 75 from the gas outlet 51B side. So that the catalyst carrier is installed in the divided flow channel 58 of the reforming flow channel 18 and the divided flow channel 64 of the combustion flow channel 20, and then the catalyst carrier 75 installed in each divided flow channel 58, 64. A reforming catalyst 22 and an oxidation catalyst 24 are supported. In order to stop the catalyst carrier at the upstream carrier end 22A and the upstream carrier end 24A (control line), a catalyst sensor 74 is disposed in a representative part or all of the divided flow paths 58 and 64 and detects the catalyst carrier. This detection signal is used. A method for manufacturing the heat exchange reformer 10 will be specifically described.

  In manufacturing the heat exchange type reformer 10, as shown in FIG. 2, the unit plate members 50 and 51 are alternately laminated, and the free end of each outer wall 54 and 60 is the plate of the adjacent unit plate members 50 and 51. Bonded to the part 52. Thereby, the laminated core part 65 is formed. Next, as shown in FIG. 5A, the catalyst carrying position sensor 74 is set in each of the divided flow paths 58 and 64 of the laminated core portion 65. The catalyst carrying position sensor 74 outputs an ON signal to not-shown notification means (display device, notification sound generating device, etc.) when the catalyst carrier comes into contact with a slurry detection unit 74A provided at the tip thereof. Therefore, in the catalyst carrying position sensor 74, the slurry detection unit 74A is positioned at the control target positions of the upstream carrying end 22A of the reforming catalyst 22 and the upstream carrying end 24A of the oxidation catalyst 24 in each of the divided flow paths 58 and 64. In addition, the gas is inserted into the representative partial flow paths 58 and 64 from the gas inlets 50A and 51A side.

  The laminated core portion 65 in which the catalyst carrying position sensor 74 is set in this way is immersed in the catalyst carrier 75 in the storage tank 76 from the gas outlet 50B and gas outlet 51B side. In the laminated core portion 65 having the microchannel structure, notification from the notification means is performed in consideration of the fact that the surface of the catalyst carrier 75 in each of the divided flow paths 58 and 64 is higher than the surface in the storage tank 76 due to capillary action. Until there is (until the catalyst carrying position sensor 74 detects the catalyst carrier 75), as shown in FIGS. 5A and 5B, the laminated core portion 65 is gradually immersed in the catalyst carrier 75 (at a low speed). Let After the operation of the notification means, the laminated core portion 65 is pulled up from the storage tank 76, and the excess catalyst carrier 75 is removed from each of the divided flow paths 58 and 64 by air blow or the like from the gas inlets 50A and 51.

  Next, as shown in FIG. 5C, the reforming catalyst 22 is supplied from the gas outlet 50 </ b> B into each divided flow path 58, and the reforming catalyst 22 is supported on the catalyst carrier 75 in each divided flow path 58. . Further, the oxidation catalyst 24 is supplied from the gas outlet 51 </ b> B into each divided flow path 64, and the oxidation catalyst 24 is supported on the catalyst carrier 75 in each divided flow path 64. Thereby, the reforming catalyst 22 is supported on the heat exchange channel 58A and the reformed gas guide channel 58C in each divided channel 58, and the reforming catalyst 22 is not supported on the reformed gas guide channel 58B. In addition, the oxidation catalyst 24 is supported on the heat exchange flow path 64A and the combustion exhaust gas guide flow path 64C in each divided flow path 64, and the laminated core portion 65 that does not support the oxidation catalyst 24 is configured on the mixed gas guide flow path 64B. Yes.

  The reforming inlet manifold 66, the combustion inlet manifold 70, the reforming outlet manifold 68, and the combustion outlet manifold 72 are joined to the openings of the gas inlets 50A and 51A and the gas outlets 50B and 51B of each layer in the laminated core portion 65. Thereby, the manufacture of the heat exchange type reformer 10 as shown in FIG. 2 is completed.

  Next, the operation of the embodiment will be described.

  In the fuel cell system 11 having the above-described configuration, the hydrocarbon raw material, water vapor (cathode offgas) is supplied from the raw material supply line 28 to the reforming passage 18 of the heat exchange reformer 10 by the operation of the raw material pump 26 and the cathode air pump 36. Is introduced. In the reforming flow path 18 of the heat exchange type reformer 10, the hydrocarbon raw material introduced while receiving heat supply from the combustion flow path 20 is brought into contact with the reforming catalyst 22 together with water vapor to satisfy the equation (1). A reforming reaction (see the above formulas (1) to (4)) including a steam reforming reaction and a partial oxidation reaction of the formula (2) is performed, and a reformed gas containing hydrogen at a high concentration is generated.

  The reformed gas generated in the reforming channel 18 is supplied to the anode electrode 14 from the fuel inlet 14 </ b> A of the anode electrode 14. In the fuel cell 12, hydrogen in the reformed gas supplied to the anode electrode 14 is protonated, and this proton moves to the cathode electrode 16 through the electrolyte and is introduced into the cathode electrode 16. React with. As the protons move, electrons flow from the anode electrode 14 toward the cathode electrode through the external conductor, and power generation is performed.

  With this power generation, in the fuel cell 12, hydrogen in the reformed gas supplied to the anode electrode 14 and oxygen in the cathode air supplied to the cathode electrode 16 are consumed according to the power generation amount (load power consumption). The cathode electrode 16 generates water (water vapor at the operating temperature). The gas containing water vapor is pushed out from the cathode electrode 16 to the water vapor supply line 40 as the cathode off gas as described above, and is introduced into the reforming flow path 18 from the water vapor inlet 18C.

  On the other hand, the gas after the hydrogen in the reformed gas is consumed according to the amount of power generated along with the power generation is discharged from the anode electrode 14 as the anode off, and this anode off gas passes through the anode off gas line 32, It is supplied to the combustion flow path 20 of the heat exchange type reformer 10. The combustion flow path 20 is supplied with the cooling off gas after cooling the fuel cell 12 from the combustion support gas supply line 46. In the combustion flow path 20, catalytic combustion occurs when the combustible component in the anode off-gas, which is fuel, is brought into contact with the oxidation catalyst 24 together with the oxygen in the cooling off-gas together with the combustion support gas. The heat generated by this catalytic combustion is supplied to the reforming flow path 18 via the plate portion 52. With this heat, the reforming flow path 18 maintains the reforming reaction, which is an endothermic reaction, and maintains the operating temperature (reformed gas temperature) at a temperature necessary for the reforming reaction.

  As described above, in the fuel cell system 11, the hydrocarbon raw material is supplied to the heat exchange type reformer 10, and each exhaust gas of the fuel cell 12 (cathode off-gas containing water vapor, anode off-gas containing combustible components, cooling containing oxygen). The operation of the heat exchange reformer 10 that generates hydrogen to be supplied to the fuel cell 12 is maintained by effectively using off gas).

  By the way, the reforming reaction in the reforming channel 18 generates an endothermic peak on the reforming raw material inlet side, that is, on the upstream supporting end 22A side of the reforming catalyst 22 supporting range. Further, the combustion reaction in the combustion flow path 20 generates a peak of heat generation on the fuel inlet side, that is, on the upstream carrying end 24A side of the oxidation catalyst 24 carrying range. For this reason, for example, in the cross-flow type heat exchange type reformer, the gas flow direction intersects between the reforming section and the heating section, so that there is a problem that a local high temperature section is generated due to the structure. Further, for example, in the counter flow type heat exchange type reformer, since the peak of the endothermic heat generation between the reforming part and the heating part occurs at the end of the heat exchange part opposite to the gas flow direction, the heat exchange in the reformer It is unsuitable as a vessel.

  Here, in the heat exchange type reformer 10, a parallel flow type heat exchanger having the same gas flow direction in the heat exchange channel 58A of the reforming channel 18 and the heat exchange channel 64A of the combustion channel 20 is used. In other words, in other words, the endothermic peak generated on the gas inlet 50A side where the reforming raw material is supplied in the reforming reaction, and the exothermic peak generated on the gas inlet 51A side where the fuel is supplied in the combustion reaction. Therefore, the heat exchange efficiency between the reforming flow path 18 and the combustion flow path 20 is improved. Thereby, in the heat exchange type reformer 10, it is possible to efficiently generate hydrogen by reforming by effectively using the heat generated in the combustion flow path 20.

  Thus, in the heat exchange type reformer 10 according to the first embodiment, the heat exchange efficiency between the combustion channel 20 and the reforming channel 18 is good.

  Further, here, in the heat exchange type reformer 10, the reformed gas guide channel 58B and the mixed gas guide flow located on the upstream side of the heat exchange channels 58A and 64A that substantially constitute a parallel flow type heat exchanger. Since the path 64B constitutes a cross-flow heat exchanging section, this heat exchange enables stable operation against fluctuations (improves robustness). FIG. 6 shows an experimental example. FIG. 6 is a diagram showing the temperature distribution of each part in the gas flow direction of the divided flow path 64 when the temperature of the supplied mixed gas is constant at 400 ° C. The solid line is a modified line supplied to the divided flow path 58. When the temperature of the raw material is 600 ° C., the broken line indicates the case where the temperature of the reforming material supplied to the divided flow path 58 is 400 ° C. From this figure, it can be seen that even if the temperature of the gas flowing into the divided flow path 58 changes by 200 ° C., the increase in the maximum temperature of the divided flow path 64 can be suppressed to 30 ° C. That is, in the heat exchange type reformer 10, a sudden change in the reaction field temperature depending on the gas inlet temperature can be effectively suppressed.

  Furthermore, in the heat exchange type reformer 10, since the reforming catalyst 22 and the oxidation catalyst 24 are not supported on the cross-flow heat exchange section formed by the reformed gas guide channel 58B and the mixed gas guide channel 64B, The reforming reaction and the combustion reaction do not occur in the reformed gas guide channel 58B and the mixed gas guide channel 64B. For this reason, generation | occurrence | production of the local high temperature site | part resulting from the imbalance of the heat | fever absorption / exothermic position which becomes a problem in a cross-flow type heat exchange type reformer is prevented. In the configuration in which the reforming catalyst 22 and the oxidation catalyst 24 are supported on the reformed gas guide channel 58B and the mixed gas guide channel 64B, the temperature of the reformed gas discharged from each divided channel 58 (reforming outlet manifold 68). The maximum temperature of the reformed gas guide channel 58B when the temperature is controlled to 650 ° C. was approximately 800 ° C., whereas in the heat exchange type reformer 10, the maximum temperature of the reformed gas guide channel 58B was the same. Experimental results with a temperature of approximately 180 ° C. were obtained.

  As described above, the cross-flow heat exchange unit (pseudo-pseudo) configured by the reformed gas guide channel 58B and the mixed gas guide channel 64B is disposed upstream of the parallel flow heat exchange unit configured by the heat exchange channel 58A and the heat exchange channel 64A. By providing the cross flow portion, an ideal reaction field (heat balance) between the reforming flow path 18 and the combustion flow path 20 can be formed, and robustness as a system can be improved. It was.

  Further, in order to control the installation range of the catalyst carrier 75, that is, the support range of the reforming catalyst 22 and the oxidation catalyst 24, using the catalyst support position sensor 74, the upstream support ends 22A and 24A of the reforming catalyst 22 and the oxidation catalyst 24 are provided. It can be formed with high accuracy. That is, in the laminated core portion 65 in which a large number of unit plate members 50 and 51 are laminated, the inside of each of the divided flow paths 58 and 64 cannot be visually observed, but by using the catalyst carrying position sensor 74, FIG. As shown in FIG. 7B, the catalyst is supported on the reformed gas guide channel 58B and the mixed gas guide channel 64B, or the amount of catalyst supported on the heat exchange channels 58A and 64A is as shown in FIG. It is possible to prevent a shortage or a significant difference in the supported ranges of the reforming catalyst 22 and the oxidation catalyst 24 as shown in FIG.

  In addition, the laminated core portion 65 of the heat exchange type reformer 10 is mixed with the reformed gas guide channel 58B positioned substantially upstream of the heat exchange channels 58A and 64A constituting the parallel flow type heat exchanger. Since the gas guide channel 64B constitutes a cross flow (pseudo-cross flow) portion, the gas inlet 50A having the same opening surface in each layer and the gas inlet 51A having the same opening surface in each layer are provided in the opening direction. Could be configured as different independent openings. As a result, the reforming inlet manifold 66 that forms the collecting space in which the gas inlet 50A of each layer opens and the collecting space in which the gas inlet 51A of each layer opens are formed in the parallel flow type with a good balance of heat absorption and heat generation as described above. A configuration for connecting the combustion inlet manifold 70 to be formed was realized. For this reason, compared with the configuration in which the reforming raw material and the mixed gas (anode off gas as fuel) are individually supplied to the gas inlets 50A and 51A of each layer, the uniformity of the flow distribution to the divided flow paths 58 and 64 is improved. Can be improved.

  In particular, by providing the combustion inlet manifold 70, the gas mixer 33 for supplying the mixed gas to each divided flow path 64 (combustion flow path 20) can be disposed immediately before the gas inlet 51A. Such a gas mixer 33 is provided downstream of a microchannel structure formed by alternately stacking unit plates such that the flow direction changing portion 52C and the outlet guide walls 56C and 62C are removed from the unit plate members 50 and 51. If configured as a mixed space, the gas mixer 33 can be disposed (configured) in the combustion inlet manifold 70 (a rectangular cross-section pipe continuous with the combustion inlet manifold 70).

  Further, in the laminated core portion 65 of the heat exchange type reformer 10, the combustion and the reformed gas guide flow channel 58C located on the downstream side of the heat exchange channels 58A and 64A that substantially constitute the parallel flow type heat exchanger and the combustion are performed. Since the exhaust gas guide channel 64C forms a cross flow (pseudo-cross flow) portion, the gas outlets 50B and 51B can be configured as independent openings having different opening directions. As a result, the reforming outlet manifold 68 that forms the collecting space in which the gas outlet 50B of each layer opens and the collecting space in which the gas outlet 51B of each layer opens are formed in a parallel flow type with a good balance of heat absorption and heat generation as described above. A configuration for connecting the combustion outlet manifold 72 to be formed was realized. For this reason, in combination with the above-described effects of installing the reforming inlet manifold 66 and the combustion inlet manifold 70, each reformed gas and combustion exhaust gas are individually discharged from the gas outlets 50B and 51B of each layer. The uniformity of flow distribution to the flow paths 58 and 64 can be further improved.

  In each of the above embodiments, the example in which the heat exchange type reformer 10 is applied to the fuel cell system 11 has been shown. However, the present invention is not limited to this, and is for obtaining a hydrogen-containing gas from a reforming raw material. Various heat exchange type reformers are sufficient, and are not limited by the application.

  Further, in each of the above embodiments, the unit plate member 50 for forming the reforming flow path 18 and the unit plate member 51 for forming the combustion flow path 20 are alternately stacked to form the heat exchange reformer 10. , 70, 80, and 90 are shown, but the present invention is not limited to this. For example, the unit in which the one-layer combustion flow path 20 is arranged with respect to the two-layer reforming flow path 18 is shown. The plate member 50 and the unit plate member 51 may be laminated.

  Further, in each of the above-described embodiments, the flow direction changing sections 52B and 52C (gas guide flow paths 58B, 64B, 58C, and 64C) having a substantially triangular shape with respect to the parallel flow section 52A (the heat exchange flow paths 58A and 64A) having a substantially rectangular shape. However, the present invention is not limited to this, and flow direction changing portions 52B and 52C having various shapes can be provided. In addition, the guide wall 56B and the like that configure the gas guide flow path 58B and the like together with the flow direction conversion unit 52B and the like are not limited to a configuration having a linear shape, and may be, for example, a curved shape.

It is a disassembled perspective view which shows the principal part of the heat exchange type | mold reformer which concerns on embodiment of this invention. It is a perspective view of the heat exchange type reformer concerning the embodiment of the present invention. It is a disassembled plan view which shows the principal part of the heat exchange type | mold reformer which concerns on embodiment of this invention. 1 is a schematic system flow diagram of a fuel cell system to which a heat exchange type reformer according to an embodiment of the present invention is applied. It is a figure which shows the catalyst carrying | support process of the heat exchange type | mold reformer which concerns on embodiment of this invention, Comprising: (A) is a schematic diagram which shows the inflow state of a catalyst carrier, (B) is a schematic diagram of the inflow stop state of a catalyst carrier. FIG. 4C is a schematic diagram of the catalyst introduction state. It is a diagram which shows the temperature distribution of the combustion flow path of the heat exchange type | mold reformer which concerns on embodiment of this invention. Each of (A) to (C) is a schematic diagram showing a failure example of catalyst support.

Explanation of symbols

10 Heat Exchange Type Reformer 18 Reforming Channel (Reforming Section)
20 Combustion flow path (heating part)
22 reforming catalyst 24 oxidation catalyst 50 unit plate member (plate member for reforming portion formation)
50A gas inlet (reforming raw material supply port)
50B Gas outlet (reformed gas outlet)
51 Unit plate member (Plate member for heating part formation)
51B Gas outlet (fuel supply port)
51A Gas inlet (exhaust port for combustion exhaust gas)
52 Plate part (flat plate part)
56 Standing wall 58 Divided flow path (reformer)
58A Heat exchange channel (Heat exchange part)
58B Reformed Raw Material Guide Channel (Reformed Raw Material Guide Section)
62 Standing wall 64 Divided flow path (heating unit)
64A heat exchange flow path (heat exchange section)
64B Mixed gas guide channel (fuel guide part)
65 Laminated core 66 Reformation inlet manifold (manifold for reforming material)
70 Combustion inlet manifold (fuel manifold)

Claims (6)

A reforming part for generating a reformed gas containing hydrogen from a reforming raw material supported by a reforming reaction including a steam reforming reaction, on which a reforming catalyst for reforming reaction is supported;
An oxidation catalyst for catalytic combustion is supported while adjoining the reforming section through a partition so as to generate a gas flow in the same direction as the gas flow of the reforming section, and accompanying the catalytic combustion of the supplied fuel A heating unit for supplying the generated heat to the reforming unit,
One end side is the reforming raw material supply port, and the other end side is a reforming raw material introduction section continuous to the reforming raw material inflow side in the reforming section,
One end side is the fuel supply port and the other end side is continuous with the fuel inflow side in the heating unit, and the fuel is supplied in a flow direction different from the flow direction of the reforming material by the reforming material introduction unit. A fuel introduction section that leads to the heating section;
A heat exchange type reformer equipped with   The heat exchange reformer according to claim 1, wherein the fuel introduction part is entirely a non-supporting region of the oxidation catalyst. A plurality of the reforming unit and the heating unit are provided so that at least a part of the reforming unit and the heating unit are adjacent to each other.
The reforming material introduction section is provided in each layer of the reforming section, and the opening surface of the reforming material supply port is matched,
3. The heat exchange reformer according to claim 1, wherein the fuel introduction section is provided in each layer of the heating section so that the opening surfaces of the fuel supply ports coincide with each other. A flat plate portion formed in a flat plate shape and a heat exchanging portion constituting the reforming portion between the flat plate portion and the reforming raw material in a predetermined direction on the supply side of the reforming raw material with respect to the heat exchanging portion A reforming portion forming plate member in which a standing wall for guiding is formed and a reforming material guide portion constituting the reforming material introducing portion is formed between the other flat plate portion,
A heat exchange part constituting the heating part between the flat plate part formed in a flat plate shape and another flat plate part, and the fuel for reforming part formation on the fuel supply side with respect to the heat exchange part A heating part forming plate member in which a standing wall that guides in a direction crossing a predetermined direction of the member is erected and a fuel guide part that constitutes the fuel introduction part is formed between the other flat plate part;
The heat exchange type | mold reformer of Claim 3 containing the lamination | stacking core part comprised by laminating | stacking by a predetermined pattern. A reforming material manifold for forming a collective space in which the reforming material supply ports of the plurality of reforming material introducing portions are opened, and for distributing and supplying the reforming materials to the plurality of reforming material introducing portions; ,
A fuel manifold for forming a collective space in which fuel supply ports of the plurality of fuel introduction portions are opened, and for distributing and supplying fuel to the plurality of fuel introduction portions;
The heat exchange reformer according to claim 3 or 4, further comprising: A reformed gas lead-out section having one end side as an outlet for the reformed gas and the other end side being continuous with the outflow side of the reformed gas in the reforming section;
One end side is a combustion exhaust gas discharge port of the heating unit and the other end side is continuous with the combustion exhaust gas discharge side of the heating unit, and the flow direction is different from the flow direction of the reformed gas by the reformed gas outlet unit A combustion exhaust gas discharge part for guiding the combustion exhaust gas to the exhaust port of the combustion exhaust gas,
The heat exchange type reformer according to any one of claims 1 to 5, further comprising:

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