JP2023133772A - Reformer and fuel cell system - Google Patents

Abstract

To provide a reformer that attains suppressed deterioration of the reforming efficiency of the reformer.SOLUTION: A reformer 10 comprises a container 12 and a cylindrical catalyst layer 20 which is located in the container 12 and filled with a catalyst 22 for reforming a source gas into a reformed gas. The source gas introduced from one axial end of the catalyst layer 20 to the hollow or outer periphery of the catalyst layer 20 flows radially through the catalyst layer 20. The catalyst layer 20 includes a plurality of partition plates 30 that divide the catalyst layer 20 into a plurality of sectional catalyst layers 20a, 20b, 20c, 20d and 20e in the axial direction.SELECTED DRAWING: Figure 2

Description

The technology disclosed herein relates to a reformer and a fuel cell system.

Patent Document 1 describes an adsorption device that includes a container and a cylindrical adsorption layer placed in the container and filled with an adsorbent that adsorbs a specific component in a mixed gas. The adsorption device of Patent Document 1, in which a mixed gas introduced from one end in the axial direction into the hollow part or the outer peripheral part of the adsorption bed flows through the catalyst bed in the radial direction, is modified by replacing the adsorbent with a catalyst. It is conceivable that it could be used as a token.

Japanese Patent Application Publication No. 1-164417

When the adsorption device described in Patent Document 1 is used as a reformer, a partition plate that divides the catalyst layer in the axial direction is not provided. Therefore, for example, when the raw material gas introduced into the hollow part or the outer peripheral part of the catalyst layer from one end in the axial direction of the catalyst layer flows through the catalyst layer in the radial direction, it tends to flow by taking a short cut in the diagonal direction. As a result, flow stagnation occurs in a portion of the catalyst layer, which may reduce the reforming efficiency.

The problem to be solved by the technology disclosed in this specification is to suppress a decrease in the reforming efficiency of a reformer.

In order to solve the above problems, the technology disclosed in this specification takes the following measures.

The first means includes a container and a cylindrical catalyst layer disposed in the container and filled with a catalyst for reforming raw material gas into reformed gas, and one axial end of the catalyst layer. A reformer in which a raw material gas introduced from the side into a hollow part or an outer peripheral part of the catalyst bed flows radially through the catalyst bed, the catalyst bed having a plurality of sections in the axial direction. This is a reformer that is provided with one or more partition plates that divide the catalyst layer.

According to the first means, the flow of the raw material gas is made uniform over the entire area of the catalyst layer by rectifying the flow of the raw material gas by one or more partition plates that divide the catalyst layer into a plurality of divided catalyst layers. . Thereby, the catalyst can be effectively utilized over the entire area of the catalyst layer. Therefore, a decrease in the reforming efficiency of the reformer can be suppressed.

The second means is the reformer of the first means, and in each of the axially adjacent sectional catalyst layers of the catalyst layer, one of the sectional catalysts located on one end side in the axial direction of the catalyst layer. This is a reformer in which the pressure drop of the layer is larger than the pressure drop of the other segmented catalyst layer.

According to the second means, in each segmented catalyst layer adjacent to each other in the axial direction of the catalyst layer, the raw material gas does not easily flow through one segmented catalyst layer, and the raw material gas easily flows through the other segmented catalyst layer. Thereby, the flow of the raw material gas flowing through each segmented catalyst layer can be made uniform.

A third means is the reformer of the second means, wherein the axial dimension of the one of the segmented catalyst layers is smaller than the axial dimension of the other segmented catalyst layer. be.

According to the third means, in each of the axially adjacent segmented catalyst layers, the axial dimension of one segmented catalyst layer is made smaller than the axial dimension of the other segmented catalyst layer. The pressure drop of one segmented catalyst layer can be made larger than the pressure drop of the other segmented catalyst layer.

A fourth means is the reformer of the second or third means, which includes an inner cylindrical part having air permeability that surrounds the inner periphery of each of the segmented catalyst layers, and an inner cylindrical part that surrounds the outer periphery of the segmented catalyst layer. It has an air permeable outer cylindrical part, and the opening area per unit area of the inner cylindrical part and/or the outer cylindrical part in the one of the sectional catalyst layers is equal to the opening area per unit area of the inner cylindrical part and/or the outer cylindrical part in the other sectional catalyst layer. The reformer has an opening area smaller than the opening area per unit area of the inner cylinder part and/or the outer cylinder part.

According to the fourth means, in each of the axially adjacent catalyst layers, the opening area per unit area of the inner cylinder part and/or the outer cylinder part in one catalyst layer is equal to the opening area per unit area of the inner cylinder part and/or the outer cylinder part in the other catalyst layer. By making the opening area smaller than the opening area per unit area of the inner cylinder part and/or the outer cylinder part, the pressure loss of one segmented catalyst layer can be made larger than the pressure loss of the other segmented catalyst layer.

A fifth means is the reformer according to any one of the first to fourth means, and is a reformer device comprising a heat transfer member that transfers heat of the reformed gas to the raw material gas. .

According to the fifth means, the heat of the reformed gas is received by the heat transfer member and the heat is transferred to the raw material gas, thereby heating the raw material gas. Thereby, reforming of the raw material gas can be promoted.

A sixth means is the reformer according to any one of the first to fifth means, wherein the minimum opening area of the passage downstream of the catalyst layer is the minimum opening area of the passage upstream of the catalyst layer. It is a reformer that is larger than the .

According to the sixth means, when the volume of the reformed gas is larger than the volume of the raw material gas, an increase in pressure in the passage on the downstream side of the catalyst layer is suppressed, and it is suppressed that the raw material gas becomes difficult to flow into the catalyst layer. can do. Furthermore, since the reforming (decomposition reaction) of the raw material gas is inhibited under high pressure, a decrease in reforming efficiency can be suppressed by lowering the pressure in the passage on the downstream side of the catalyst layer.

A seventh means is the reformer of any one of the first to sixth means, and is a reformer equipped with a heating device that heats each of the segmented catalyst layers.

According to the seventh means, reforming of the catalyst can be promoted by heating each segmented catalyst layer with each heating device.

An eighth means is the reformer of the seventh means, and includes a temperature sensor that detects the temperature of each of the divided catalyst layers, and controls energization of each of the heating devices based on detection information of each of the temperature sensors. This is a reformer equipped with a control device for controlling.

According to the eighth means, the control device controls the energization of each heating device based on the detection information of each temperature sensor. Thereby, the temperature of each section catalyst layer can be optimized and unnecessary heating can be suppressed. In other words, energy saving can be achieved by thermally managing each segmented catalyst layer.

A ninth means includes the reformer according to any one of claims 1 to 8, which reformes ammonia as the raw material gas into the reformed gas containing hydrogen and nitrogen; This fuel cell system includes an adsorption device that adsorbs ammonia, and a fuel cell that generates electricity using hydrogen obtained by the adsorption device as fuel.

According to the eighth means, reformed gas is obtained by a reformer that can suppress a decrease in reforming efficiency, and hydrogen as a purified gas in which specific components of the reformed gas are adsorbed by an adsorption device is used as fuel. A fuel cell generates electricity.

According to the technology disclosed in this specification, it is possible to suppress a decrease in the reforming efficiency of the reformer.

1 is a schematic diagram showing an overview of a fuel cell system according to a first embodiment; FIG. It is a sectional view showing a reformer. FIG. 3 is a sectional view showing a reformer according to a second embodiment. FIG. 3 is a sectional view showing a reformer according to a third embodiment.

Hereinafter, embodiments for implementing the technology disclosed in this specification will be described using the drawings.

[Embodiment 1]
In this embodiment, a reformer used in a fuel cell system using hydrogen as fuel will be exemplified.

(Overview of fuel cell system)
FIG. 1 is a schematic diagram showing an overview of a fuel cell system. As shown in FIG. 1, the fuel cell system 100 includes a reformer 10, an ammonia adsorption device (hereinafter referred to as "adsorption device") 102, and a fuel cell (FC) 104.

The reformer 10 uses pure ammonia (NH3) as a raw material gas and includes a reforming catalyst that reformes (decomposes) ammonia into hydrogen and nitrogen through a thermal decomposition reaction. The components of the reformed gas obtained by the reformer 10 are mainly hydrogen and nitrogen, and also include ammonia that did not contribute to the reforming reaction. The reformed gas is supplied to the adsorption device 102.

The adsorption device 102 adsorbs ammonia contained in the reformed gas supplied from the reformer 10. The purified gas from which ammonia has been removed by the adsorption device 102 is supplied to the fuel cell 104 . The components of purified gas are mainly hydrogen and nitrogen.

The fuel cell 104 uses purified gas hydrogen as fuel to generate electricity. By removing ammonia by the adsorption device 102, deterioration of the stack of the fuel cell 104 is suppressed.

(Reformer 10)
FIG. 2 is a sectional view showing the reformer 10. In FIG. 2, the left side is the front and the right side is the rear. As shown in FIG. 2, the reformer 10 includes a cylindrical container 12 and a cylindrical catalyst layer 20 provided concentrically within the container 12.

The container 12 has a container body 13 and a lid plate 14. The container body 13 is formed by closing one end opening (front end opening) of a cylindrical tube portion 13a with a disc-shaped end wall portion 13b. The other open end (rear end opening) of the cylindrical portion 13 a is closed by a cover plate 14 .

A cylindrical introduction port 16 that communicates between the inside and outside of the container 12 protrudes concentrically from the center of the rear surface of the lid plate 14 . A cylindrical outlet port 18 that communicates between the inside and outside of the container 12 is protruded from the outer periphery of the rear side of the lid plate 14 (the lower part in FIG. 2). The outlet 18 has a diameter 18d larger than the diameter 16d of the inlet 16. The rear side of the container 12 corresponds to "one axial end side" in this specification. The front side of the container 12 corresponds to the "other axial end side" in this specification.

A heat transfer member 50 is provided within the rear end (right end in FIG. 2) of the container 12. The heat transfer member 50 includes a cylindrical connecting tube 50a and a plurality (for example, four) of annular plate-shaped heat receiving plates 50b. A rear end portion (right end portion in FIG. 2) of the connecting tube 50a is continuously connected to the introduction port 16. The inner circumferential end of each heat receiving plate 50b is connected to the connecting tube 50a. The heat receiving plates 50b are arranged in parallel at equal intervals in the axial direction. The heat receiving plate 50b corresponds to a "heat receiving member" in this specification.

The heat receiving plate 50b at the front end (the left end in FIG. 2) is arranged so that its front surface is flush with the front end surface of the connecting tube 50a. The heat receiving plate 50b at the rear end (right end in FIG. 2) is arranged to face the lid plate 14 with a predetermined distance therebetween. The outer diameter of the heat receiving plate 50b is smaller than the inner diameter of the cylindrical portion 13a of the container body 13. In this embodiment, the outer diameter of the heat receiving plate 50b is approximately equal to the outer diameter of the outer cylinder portion 26 (described later).

A cylindrical space corresponding to the catalyst layer 20 is formed inside the container 12 . The cylindrical space is formed by the heat receiving plate 50b at the front end of the heat transfer member 50, the inner cylinder part 24, the outer cylinder part 26, and the end plate part 28. A cylindrical space is filled with a granular reforming catalyst (hereinafter referred to as "catalyst") 22. A catalyst layer 20 is formed by the catalyst 22 . The catalyst 22 is capable of reforming (decomposing) ammonia into hydrogen and nitrogen. Further, the catalyst 22 contains, for example, nickel (Ni), palladium (Pd), ruthenium (Ru), and the like.

The inner cylinder portion 24 is formed into a cylindrical shape. The inner cylinder part 24 is arranged concentrically within the container 12. A rear end portion (right end portion in FIG. 2) of the inner cylinder portion 24 is continuously connected to a connecting cylinder 50a of the heat transfer member 50. A series of source gas passages 25 are formed by the inner cylinder part 24, the connecting cylinder 50a of the heat transfer member 50, and the hollow part of the introduction port 16. In the source gas passage 25, the opening area of the inlet 16 corresponds to the minimum opening area. The raw material gas passage 25 corresponds to the "passage upstream of the catalyst layer" in this specification. The hollow portion of the inner cylinder portion 24 corresponds to the “hollow portion of the catalyst layer” in this specification.

Moreover, the inner cylinder part 24 is formed in a mesh shape and has breathability. Note that the pore diameter, pitch, aperture ratio, etc. of the mesh of the inner cylindrical portion 24 can be set as appropriate. Furthermore, the size of the pores in the mesh may be larger than the size of the catalyst 22. In this case, in order to prevent the catalyst 22 from spilling, it is preferable to provide a filter member such as glass wool surrounding the outer circumferential surface or inner circumferential surface of the inner cylinder part 24, for example.

The outer cylinder part 26 is formed into a cylindrical shape surrounding the inner cylinder part 24 at a predetermined interval. The outer cylindrical portion 26 is arranged at a predetermined distance from the cylindrical portion 13a of the container body 13. That is, the outer cylinder part 26 is arranged so as to form a triple cylinder shape with the inner cylinder part 24 and the cylinder part 13a. The outer cylinder part 26 is arranged between the heat receiving plate 50b at the front end of the heat transfer member 50 and the end plate part 28. The space between the cylindrical portion 13a of the container body 13 and the outer cylindrical portion 26 corresponds to the "outer periphery of the catalyst layer" in this specification.

Further, the outer cylinder portion 26 is divided into a plurality of (for example, five) short cylinder portions 26a, 26b, 26c, 26d, and 26e in the axial direction (front-back direction). The short cylindrical portion 26a at the front end is connected to the end plate portion 28. The short cylindrical portion 26e at the rear end is connected to the heat receiving plate 50b at the front end of the heat transfer member 50.

The axial dimensions La, Lb, Lc, Ld, and Le of each short cylindrical portion 26a, 26b, 26c, 26d, and 26e are gradually increased (longer) from the rear (dimension Le side) to the front (dimension La side). ).

Each short cylinder part 26a, 26b, 26c, 26d, 26e is formed in a mesh shape and has breathability. Note that the pore diameter, pitch, aperture ratio, etc. of the mesh of each of the short cylindrical portions 26a, 26b, 26c, 26d, and 26e can be set as appropriate. Furthermore, the size of the pores in the mesh may be larger than the size of the catalyst 22. In this case, in order to prevent spillage of the catalyst 22, a filter member such as glass wool may be provided to surround the outer or inner circumferential surface of each of the short cylinder portions 26a, 26b, 26c, 26d, and 26e.

The end plate portion 28 is formed into a disk shape. The end plate part 28 is arranged so as to close the front end opening between the inner cylinder part 24 and the outer cylinder part 26. The rear end openings of the inner cylinder part 24 and the outer cylinder part 26 are closed by a heat receiving plate 50b at the front end of the heat transfer member 50.

The end plate portion 28 is disposed to face the end wall portion 13b of the container body 13 with a predetermined gap in the axial direction (front-back direction). In the container 12, there is a space on the outer circumference side of the outer cylinder part 26, a space on the outer circumference side of the heat transfer member 50 (a space between adjacent heat receiving plates 50b, and a rear end heat receiving plate 50b and a lid plate). 14) and the hollow part of the outlet port 18, a series of reformed gas passages 29 are formed. In the reformed gas passage 29, the opening area of the outlet 18 corresponds to the minimum opening area. The reformed gas passage 29 corresponds to "a passage downstream of the catalyst layer" in this specification.

The catalyst layer 20 is partitioned into a plurality (for example, five) of partition plates 30 in the form of a plurality of annular plates (for example, four). That is, between the adjacent short cylinder parts 26a and 26b of the outer cylinder part 26, between the short cylinder parts 26b and 26c, between the short cylinder parts 26c and 26d, and between the short cylinder parts 26a and 26b, A partition plate 30 is arranged between the portion 26d and the short cylindrical portion 26e. The inner circumferential end of each partition plate 30 is connected to the inner cylindrical portion 24 . The outer circumferential end of each partition plate 30 is connected to each short cylindrical portion 26a, 26b, 26c, 26d, and 26e. The partition plates 30 are arranged in parallel with each other at a predetermined interval.

Each partition plate 30 divides the catalyst layer 20 into a plurality of (for example, five) segmented catalyst layers 20a, 20b, 20c, 20d, and 20e in the axial direction (front-back direction). Note that among the segmented catalyst layers 20a, 20b, 20c, 20d, and 20e, the segmented catalyst layer 20a and the segmented catalyst layer 20b, the segmented catalyst layer 20b and the segmented catalyst layer 20c, and the segmented catalyst layer 20c are adjacent to each other in the axial direction (front-back direction). 20c and the segmented catalyst layer 20d, and the segmented catalyst layer 20d and the segmented catalyst layer 20e, the rear segmented catalyst layer corresponds to "one segmented catalyst layer located at one end in the axial direction of the catalyst layer", and the front segmented catalyst layer corresponds to "one segmented catalyst layer located at one end in the axial direction of the catalyst layer" The layer corresponds to "the other segmented catalyst layer".

The axial dimensions La, Lb, Lc, Ld, and Le of each of the short cylindrical portions 26a, 26b, 26c, 26d, and 26e of the outer cylindrical portion 26 gradually increase (lengthen) from the rear toward the front. Therefore, the axial dimension of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e increases (longens) stepwise from the rear (dimension Le side) to the front (dimension La side).

Thereby, the pressure loss of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e becomes smaller stepwise from the rear toward the front. That is, in each of the catalyst layer sections 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e adjacent to each other in the axial direction of the catalyst layer 20, the pressure loss in one (rear) section is lower than that in the other (front) section. It is larger than the pressure drop of the catalyst layer.

The opening area per unit area of each portion of the inner cylinder portion 24 surrounding the inner periphery of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e (each portion corresponding to each segmented catalyst layer) is determined from the rear to the front. It is set to increase in stages. Thereby, the pressure loss of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e becomes smaller stepwise from the rear toward the front. That is, in each of the catalyst layer sections 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e adjacent to each other in the axial direction of the catalyst layer 20, the pressure loss in one (rear) section is lower than that in the other (front) section. It is larger than the pressure drop of the catalyst layer.

In the outer cylindrical portion 26 surrounding the outer periphery of each segmented catalyst layer 20a, 20b, 20c, 20d, 20e, per unit area of each portion (each short cylindrical portion 26a, 26b, 26c, 26d, 26e) The opening area is set to increase stepwise from the rear to the front. Thereby, the pressure loss of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e becomes smaller stepwise from the rear toward the front. That is, in each of the catalyst layer sections 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e adjacent to each other in the axial direction of the catalyst layer 20, the pressure loss in one (rear) section is lower than that in the other (front) section. It is larger than the pressure drop of the catalyst layer.

The container 12, the inner cylinder part 24, the outer cylinder part 26 (each short cylinder part 26a, 26b, 26c, 26d, 26e), the end plate part 28, each partition plate 30, and the heat transfer member 50 have a thermal conductivity of the catalyst 22. They are each made of a metal material, such as stainless steel, that has a higher thermal conductivity. Further, it is preferable to use a metal material having higher thermal conductivity than the container 12 and other members for the heat transfer member 50.

(Effect of reformer 10)
Raw material gas (ammonia) is introduced into the raw material gas passage 25. The raw material gas flows radially outward in each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e. At this time, ammonia is decomposed (reformed) into hydrogen and nitrogen by the catalysts 22 of the respective segmented catalyst layers 20a, 20b, 20c, 20d, and 20e, resulting in a reformed gas. Thereafter, the reformed gas flows through the reformed gas passage 29 and is then supplied to the adsorption device 102 (see FIG. 1).

Further, the reformed gas flowing through the reformed gas passage 29 comes into contact with the outer surface of the heat transfer member 50 . As a result, the heat of the reformed gas is received by the heat transfer member 50, and the heat is transferred to the source gas flowing through the source gas passage 25 (specifically, the hollow part of the connecting tube 50a of the heat transfer member 50). The raw material gas is heated. In FIG. 2, the flow of the raw material gas is shown by arrows.

(Advantages of Embodiment 1)
According to this embodiment, the flow of the raw material gas is rectified by the plurality of partition plates 30 that divide the catalyst layer 20 into a plurality of segmented catalyst layers 20a, 20b, 20c, 20d, and 20e. In other words, the flow shortcut that occurred in Patent Document 1 is suppressed. Therefore, the flow of raw material gas to the entire area of the catalyst layer 20 (all the segmented catalyst layers 20a, 20b, 20c, 20d, and 20e) is made uniform. Thereby, the catalyst 22 can be effectively utilized across all the segmented catalyst layers 20a, 20b, 20c, 20d, and 20e. Therefore, a decrease in the reforming efficiency of the reformer 10 can be suppressed.

Also, in each of the axially adjacent segmented catalyst layers 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e of the catalyst layer 20, the pressure loss of one (rear) segmented catalyst layer is greater than that of the other (front) segmented catalyst layer. It is larger than the pressure drop of the segmented catalyst layer. Therefore, the raw material gas does not easily flow through one (rear side) segmented catalyst layer, and the raw material gas easily flows through the other (front side) segmented catalyst layer. Thereby, the flow of the raw material gas flowing through each of the segmented catalyst layers 20a, 20b, 20c, 20d, and 20e can be made uniform.

In addition, in each of the axially adjacent segmented catalyst layers 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e of the catalyst layer 20, the axial dimension of one (rear side) segmented catalyst layer is set to the other (front side). By making the axial dimension smaller than the axial dimension of the segmented catalyst layer, the pressure loss of one (rear) segmented catalyst layer can be made larger than the pressure loss of the other (front) segmented catalyst layer.

In addition, in each of the axially adjacent sectional catalyst layers 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e of the catalyst layer 20, each portion of the inner cylinder portion 24 in one (rear) sectional catalyst layer is By making the opening area per unit area smaller than the opening area per unit area of each part of the inner cylinder part 24 in the other (front) segmented catalyst layer, the pressure loss in one (rear) segmented catalyst layer can be reduced. The pressure drop can be made larger than the pressure loss of the other (front side) segmented catalyst layer.

In addition, in each of the axially adjacent sectional catalyst layers 20a, 20b, 20b, 20c, 20c, 20d, 20d, and 20e of the catalyst layer 20, each short tube of the outer cylindrical portion 26 in one (rear) sectional catalyst layer is By making the opening area per unit area of the section smaller than the opening area per unit area of each short cylinder part of the outer cylinder part 26 in the other (front side) partitioned catalyst layer, one (rear side) partitioned catalyst layer The pressure drop of the layer can be made larger than the pressure drop of the other (front side) segmented catalyst layer.

Further, the heat of the reformed gas is received by the heat transfer member 50, and the heat is transferred to the raw material gas, thereby heating the raw material gas. Thereby, reforming of the raw material gas can be promoted.

Further, the minimum opening area of the reformed gas passage 29 is larger than the minimum opening area of the raw material gas passage 25. Therefore, when the volume of the reformed gas is larger than the volume of the raw material gas, it is possible to suppress an increase in pressure in the reformed gas passage 29 and to prevent the raw material gas from flowing into the catalyst layer 20 more easily.

For example, in the case of an ammonia decomposition reaction represented by 2NH3→N2+3H2, the volume of the reformed gas increases to twice the volume of the raw material gas. Then, if the minimum opening area of the raw material gas passage 25 and the minimum opening area of the reformed gas passage 29 are equal, the pressure of the reformed gas passage 29 increases, and the raw material gas is transferred from the raw material gas passage 25 to the catalyst layer 20. This causes a problem in which it becomes difficult for the water to flow into the tank. However, such a problem can be improved by making the minimum opening area of the reformed gas passage 29 larger than the minimum opening area of the raw material gas passage 25.

Further, since reforming (decomposition reaction) of the raw material gas is inhibited under high pressure, by lowering the pressure in the reformed gas passage 29, it is possible to suppress a decrease in reforming efficiency.

Further, the fuel cell system 100 includes a reformer 10 that reforms ammonia as a raw material gas into a reformed gas containing hydrogen and nitrogen, an adsorption device 102 that adsorbs ammonia in the reformed gas, and a and a fuel cell 104 that generates electricity using the generated hydrogen as fuel. Therefore, reformed gas is obtained by the reformer 10 that can suppress a decrease in reforming efficiency, and the fuel cell 104 is powered by hydrogen as a purified gas in which specific components of the reformed gas have been adsorbed by the adsorption device 102. generates electricity.

[Embodiment 2]
Since this embodiment is a modification of the reformer 10 of Embodiment 1, the modified parts will be explained, and the same parts as in Embodiment 1 will be given the same reference numerals and redundant explanation will be omitted. . FIG. 3 is a sectional view showing the reformer 10.

As shown in FIG. 3, an annular plate-shaped heater 40 is provided concentrically on one or both sides of each partition plate 30. For example, heaters 40 are arranged on both the front and rear sides of the partition plate 30 at the front end. A heater 40 is arranged on the rear surface of the remaining three partition plates 30. Each heater 40 is covered by the catalyst 22 of each segmented catalyst layer 20a, 20b, 20c, 20d, 20e. Each heater 40 generates heat when energized, and heats the catalyst 22 of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e. Each heater 40 is energized and controlled by a control device (ECU) 42. The heater 40 corresponds to a "heating device" in this specification. The ECU 42 corresponds to a "control device" in this specification.

The reformer 10 is provided with a temperature sensor 44 that detects the temperature of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e. Each temperature sensor 44 detects the temperature of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e, and inputs the detected information to the ECU 42. The ECU 42 individually controls the energization of each heater 40 based on the detection information of each temperature sensor 44 .

According to this embodiment, reforming of the catalyst 22 can be promoted by heating each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e with each heater 40.

Further, the ECU 42 controls energization of each heater 40 based on the detection information of each temperature sensor 44. Thereby, the temperature of each sectioned catalyst layer 20a, 20b, 20c, 20d, and 20e can be optimized and unnecessary heating can be suppressed. That is, energy saving can be achieved by thermally managing each of the segmented catalyst layers 20a, 20b, 20c, 20d, and 20e.

[Embodiment 3]
Since this embodiment is a modification of the reformer 10 of Embodiment 2, the modified parts will be explained, and the same parts as in Embodiment 2 will be given the same reference numerals and redundant explanation will be omitted. . FIG. 4 is a sectional view showing the reformer 10. As shown in FIG. 4, in this embodiment, each heater 40 (designated with the same reference numeral as in Embodiment 2) is arranged at the center of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e. Further, each temperature sensor 44 (designated with the same reference numeral as in the second embodiment) is arranged to detect the temperature of each partition plate 30. In this case, each temperature sensor 44 can detect the temperature of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e via each partition plate 30. Note that each temperature sensor 44 may be arranged similarly to the second embodiment (see FIG. 3).

[Other embodiments]
The technology disclosed in this specification is not limited to the embodiments described above, and can be implemented in various other forms. For example, the reformer 10 can be used not only for ammonia but also for various raw material gases. Further, in the embodiment, the raw material gas flows radially outward in the radial direction through the catalyst layer 20 from the hollow part side (the raw material gas passage 25 side), but depending on the raw material gas, the direction in which the raw material gas flows may be changed. You can do it the other way around. That is, the raw material gas may flow through the catalyst layer 20 in a convergent manner from the outer circumferential side toward the radially inward side. Furthermore, although the inlet 16 and the outlet 18 of the container 12 are arranged on the lid plate 14 in the embodiment, they may be arranged on the end wall 13b, or both the ports 16 and 18 are arranged separately in different parts. You may.

Further, the container 12 is not limited to a cylindrical shape, but may be a rectangular tube shape. Moreover, the number of partition plates 30 may be one. Moreover, the inner cylinder part 24 may be formed by being divided into a plurality of parts in the axial direction. Further, the outer cylinder portion 26 may be formed of one member. In addition, the pressure loss of each segmented catalyst layer 20a, 20b, 20c, 20d, and 20e is calculated based on the axial dimension of each segmented catalyst layer, the opening area per unit area of each portion of the inner cylinder portion 24 in each segmented catalyst layer, and each segmented catalyst layer. It may be changed by at least one of the opening areas per unit area of each part (each short cylinder part) of the outer cylinder part 26 in the catalyst layer. Furthermore, the shape, number, and arrangement of the heaters 40 are arbitrary. The number of heat receiving plates 50b of the heat transfer member 50 may be one. Further, the heat receiving plate 50b of the heat transfer member 50 may be replaced with a fin type or pipe type heat receiving member.

10 Reformer 12 Container 20 Catalyst layers 20a, 20b, 20c, 20d, 20e Segmented catalyst layer 22 Catalyst 24 Inner cylinder portion 25 Raw material gas passage (passage upstream of the catalyst layer)
26 Outer cylinder part 29 Reformed gas passage (passage downstream from the catalyst layer)
30 Partition plate 40 Heater (heating device)
42 ECU (control unit)
44 Temperature sensor 50 Heat transfer member 100 Fuel cell system 102 Adsorption device 104 Fuel cell

Claims (9)

a container and
a cylindrical catalyst layer disposed in the container and filled with a catalyst for reforming raw material gas into reformed gas;
It is equipped with
A reformer in which a raw material gas introduced from one axial end side of the catalyst layer into a hollow portion or an outer peripheral portion of the catalyst layer flows through the catalyst layer in a radial direction,
A reformer, wherein the catalyst layer is provided with one or more partition plates that divide the catalyst layer into a plurality of segmented catalyst layers in the axial direction. The reformer according to claim 1,
In each of the segmented catalyst layers adjacent in the axial direction of the catalyst layer, the pressure drop of one of the segmented catalyst layers located on one end side in the axial direction of the catalyst layer is larger than the pressure drop of the other segmented catalyst layer. A pawn. The reformer according to claim 2,
The axial dimension of the one of the segmented catalyst layers is smaller than the axial dimension of the other segmented catalyst layer. The reformer according to claim 2 or 3,
It has an inner cylindrical part having air permeability surrounding the inner periphery of each of the sectional catalyst layers, and an outer cylindrical part having air permeability surrounding the outer periphery of the sectional catalyst layer,
The opening area per unit area of the inner cylinder part and/or the outer cylinder part in the one segmented catalyst layer is equal to the unit area of the inner cylinder part and/or the outer cylinder part in the other segmented catalyst layer. The reformer has a smaller opening area than the actual opening area. The reformer according to any one of claims 1 to 4,
A reformer comprising a heat transfer member that transfers heat of the reformed gas to the raw material gas. The reformer according to any one of claims 1 to 5,
A reformer, wherein a minimum opening area of a passage downstream of the catalyst layer is larger than a minimum opening area of a passage upstream of the catalyst layer. The reformer according to any one of claims 1 to 6,
A reformer comprising a heating device that heats each of the segmented catalyst layers. The reformer according to claim 7,
a temperature sensor that detects the temperature of each of the divided catalyst layers;
a control device that controls energization of each of the heating devices based on detection information of each of the temperature sensors;
A reformer equipped with The reformer according to any one of claims 1 to 8, which reformes ammonia as the raw material gas into the reformed gas containing hydrogen and nitrogen;
an adsorption device that adsorbs ammonia in the reformed gas;
a fuel cell that generates electricity using hydrogen obtained by the adsorption device as fuel;
A fuel cell system equipped with

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