JP2023076221A - Fuel gas reformer - Google Patents

Abstract

To provide a fuel gas reformer capable of minimizing temperature difference in a fuel gas-reforming reaction due to a position in a honeycomb support body as much as possible.SOLUTION: A fuel gas reformer 11 includes: an inflow cell 16 that has an opened upstream end and a sealed downstream end; an outflow cell 17 that has an opened downstream end and a sealed upstream end; porous honeycomb support body 12 having a partition wall 18 separating the inflow cell 16 and the outflow cell 17; and an ATR catalyst layer 26, supported on the honeycomb support body 12, for reforming fuel gas. The ATR catalyst layer 26 is supported on the partition wall 18.SELECTED DRAWING: Figure 3

Description

The present invention relates to a fuel gas reformer.

BACKGROUND ART As a conventional fuel gas reforming device, for example, the technology described in Patent Document 1 is known. The reformer described in Patent Document 1 is a device that supplies ammonia and an oxygen-containing gas and produces hydrogen through a reforming reaction. The reformer uses a honeycomb catalyst that promotes an autothermal reforming (ATR) reaction.

Further, Patent Literature 2 describes an ammonia reforming catalyst. In Patent Literature 2, ammonia and oxygen-containing gas pass from the inlet to the outlet of the reactor supporting the ammonia reforming catalyst, so a combustion reaction is likely to occur near the inlet. Therefore, the temperature near the inlet is about 200° C. higher than that near the outlet.

JP 2015-188820 A JP 2010-214225 A

The technique described in Patent Document 2 is intended to control the temperature rise of the catalyst layer and prevent damage to the reformer and deterioration of the catalyst. Therefore, there is a problem that damage and deterioration of the reformer cannot be sufficiently prevented. In order to solve the above problem, it is conceivable to lower the temperature of the reformer, but in this case, the temperature around the outlet of the reactor becomes low, resulting in deterioration of reforming efficiency. The technology disclosed in Patent Document 1 does not mention anything about preventing damage and deterioration of the reformer caused by temperature differences.

The present invention has been made in view of the above problems, and an object of the present invention is to provide a fuel gas reforming apparatus capable of minimizing the temperature difference due to reaction in a honeycomb carrier. .

In order to solve the above problems, the present invention provides an inflow cell having an open upstream end and a plugged downstream end, and an inflow cell having an open downstream end and an upstream end. A porous honeycomb carrier having outflow cells with plugged portions and partition walls partitioning the inflow cells and outflow cells; and an ATR catalyst supported on the honeycomb carrier and reforming fuel gas. The fuel gas reformer provided therein is characterized in that the ATR catalyst is supported on the partition wall.

In such a reformer, the fuel gas flows into the inflow cells, passes through the partition walls, and flows out to the outflow cells. By arranging the inflow cells, the partition walls, and the outflow cells, the locations through which the fuel gas passes are less likely to be biased within the partition walls. This is because the partition wall causes a high pressure loss, so that the fuel gas spreads throughout the space of the inflow cell and then passes through almost the entire partition wall. The partition walls carry an ATR catalyst. Since the location where the fuel gas passes through the partition is less likely to be biased, the temperature difference in the partition can be minimized.

In the above fuel gas reformer, the partition wall has an inflow cell side wall portion facing the inflow cell and an outflow cell side wall portion facing the outflow cell, and the ATR catalyst has the inflow cell side wall portion facing the outflow cell. It is good also as a structure carried by.
In such a configuration, the ATR catalyst is carried on the side walls of the inflow cells, so even if the ATR catalyst, which may cause flaking, is used, flaking powder will not flow out to the outflow cells.

Further, in the fuel gas reformer described above, the ATR catalyst may be supported on the outflow cell side wall.
In such a configuration, the ATR catalyst is carried on the inflow cell side wall and the outflow cell side wall, so that the amount of the ATR catalyst can be increased. Then, reforming efficiency can be improved.

Further, in the fuel gas reforming apparatus described above, the ATR catalyst may have a combustion catalyst, and the combustion catalyst may be supported on the side walls of the inflow cells.
With such a configuration, heat necessary for reforming the fuel gas can be obtained in the inflow cell, so reforming efficiency can be improved.

In the above fuel gas reformer, the material of the ATR catalyst supported on the inflow cell side wall may be different from the material of the ATR catalyst supported on the outflow cell side wall.
With such a configuration, a suitable catalyst can be selected for each of the inflow cell side and the outflow cell side, so the reforming efficiency can be further improved.

Further, in the fuel gas reforming apparatus described above, the ATR catalyst may be supported on the inflow cell side wall portion and the inside of the partition wall excluding the inflow cell side wall portion.
In such a configuration, the ATR catalyst is carried inside the partition walls, and the amount of the ATR catalyst can be further increased, so that the reforming efficiency can be further improved.

Further, in the fuel gas reforming device described above, the ATR catalyst may have a combustion catalyst for burning the fuel gas, and the combustion catalyst may be supported only on the side walls of the inflow cells.
With such a configuration, heat necessary for reforming the fuel gas can be obtained in the inflow cell, so reforming efficiency can be improved. In addition, since the ATR catalyst is carried inside the partition walls, the amount of the ATR catalyst can be further increased, so that the reforming efficiency can be further improved.

According to the present invention, it is possible to provide a fuel gas reformer capable of minimizing the temperature difference due to reaction in the honeycomb carrier.

BRIEF DESCRIPTION OF THE DRAWINGS It is a perspective view which shows typically the ammonia gas reformer which concerns on 1st Embodiment. It is a front view which shows the upstream end part of an ammonia gas reformer. FIG. 3 is a view taken along the line AA in FIG. 2; (a) is an enlarged view in FIG. 2, and (b) is a view taken along line AA in FIG. 4(a). It is a graph which shows the change of temperature from the inlet side of an ammonia gas reformer to the outlet side. (a) is a cross-sectional view showing a layered structure according to a second embodiment, and (b) is a view taken along line CC in FIG. 6(a). (a) is a cross-sectional view showing a layer structure according to a third embodiment, and (b) is a view taken along line DD in FIG. 7(a). (a) is a cross-sectional view showing a layer structure according to a fourth embodiment, and (b) is a view taken along line EE in FIG. 8(a). (a) is a cross-sectional view showing a layered structure according to a fifth embodiment, and (b) is a view taken along line GG in FIG. 9(a).

(First embodiment)
A first embodiment of the present invention will be described below with reference to the drawings. In this embodiment, an ammonia gas reforming device as a fuel gas reforming device using ammonia gas as fuel gas will be described.

As shown in FIG. 1, the ammonia gas reformer 11 of this embodiment has a honeycomb carrier 12 made of porous ceramic having a honeycomb structure. The honeycomb carrier 12 has a first end face 13 as one end face, a second end face 14 as the other end face, and a cylindrical outer peripheral wall 15 .

As shown in FIGS. 1 and 2 , the honeycomb carrier 12 has a plurality of inflow cells 16 , a plurality of outflow cells 17 and partition walls 18 . As shown in FIG. 3, the inflow cell 16 is disposed inside the outer peripheral wall 15 and extends from the first end face 13 to the second end face 14, the opening of the second end face 14 being plugged by the outflow plug 19. cell. The outflow cell 17 is adjacent to the inflow cell 16 , extends from the first end surface 13 to the second end surface 14 , and has an opening in the first end surface 13 plugged with an inflow plug 20 .

Partitions 18 define a plurality of inflow cells 16 and outflow cells 17 . A plurality of inflow cells 16 and outflow cells 17 are arranged in a grid pattern by being partitioned by partition walls 18 . Therefore, as shown in FIG. 2, the inflow cells 16 and the outflow cells 17 are alternately arranged on the first end face 13 in a checkered pattern. The partition wall 18 is surrounded by the cylindrical outer wall 15, so that the honeycomb carrier 12 is formed in a columnar shape. The honeycomb carrier 12 of this embodiment is a wall flow type honeycomb carrier in which fluid flows from the inflow cells 16 to the outflow cells 17 . The flow of ammonia gas is indicated by arrow F in FIG.

As shown in FIG. 4, septum 18 includes inlet cell sidewall 22 including surface 21 facing inlet cell 16, outlet cell sidewall 24 including surface 23 facing outlet cell 17, inlet cell sidewall 22 and outlet cell sidewall 22 including surface 23 facing outlet cell 17. It has an inner wall portion 25 excluding the cell side wall portion 24 .

The honeycomb carrier 12 of the present embodiment is made of porous ceramics, but as the material, for example, cordierite, mullite, and silicon nitride ceramics having excellent heat resistance may be used, and a plurality of ceramics may be used. Combination materials may also be used. The material of the honeycomb carrier 12 preferably contains at least one selected from the group consisting of cordierite, silicon carbide, silicon nitride and mullite. More specifically, a material containing 20% by mass or more of the materials listed in this group is preferable, a material containing 30% by mass or more is more preferable, and a material containing 50% by mass or more is particularly preferable. . The honeycomb carrier 12 is obtained by extrusion-molding a ceramic material containing water and a binder and kneading it with an extruder, cutting the extrusion-molded body, drying it, and firing it after drying.

The ammonia gas reformer 11 has an ATR catalyst supported on the honeycomb carrier 12 in addition to the honeycomb carrier 12 . An ATR catalyst is a catalyst that reforms ammonia gas in an autothermal reformer (ATR). The ATR catalyst burns the ammonia gas in a temperature range of about 200° C. to 400° C., for example, and reforms the ammonia gas in a temperature range higher than the combustion temperature of the ammonia gas (eg, about 250° C. to 500° C.). It includes a combustion catalyst that burns ammonia gas and a reforming catalyst that reforms ammonia gas into hydrogen. V, Cr, Mn, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, W, Re, Os, Ir, and Pt can be used as catalytic metals for the combustion catalyst. Moreover, V, Cr, Mn, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, W, Re, Os, Ir, and Pt can be used as catalytic metals of the reforming catalyst.

As shown in FIG. 4, the ATR catalyst in this embodiment is carried as an ATR catalyst layer 26 on the inflow cell side wall portion 22 . The ATR catalyst is obtained by applying a catalyst slurry to the inflow cell side wall 22 by a wash coat method, removing excess ATR catalyst by air blow, drying the ATR catalyst at 120° C., and repeating the application and drying of the catalyst slurry. , the required amount is carried. Then, the honeycomb carrier 12 is fired, and the ATR catalyst layer 26 is formed by performing a reduction treatment after the firing.

An ammonia supplier (not shown) for storing ammonia and an air supplier (not shown) for supplying air are provided upstream of the ammonia gas reformer 11 of the present embodiment. there is Further, downstream of the ammonia gas reformer 11, a reformed gas utilization device (not shown) that utilizes the reformed gas reformed by the ammonia gas reformer 11 is provided. Therefore, ammonia gas obtained by mixing ammonia and air is supplied to the ammonia gas reforming device 11, and the ammonia gas reforming device 11 reforms the ammonia gas to generate a reformed gas. The reformed gas produced is utilized in the reformed gas utilization device.

Next, reforming of ammonia gas by the ammonia gas reforming apparatus 11 according to this embodiment will be described. First, ammonia gas mixed with ammonia and air is supplied from the upstream side of the ammonia gas reformer 11 toward the ammonia gas reformer 11 . Therefore, the ammonia gas supplied to the ammonia gas reforming device 11 flows into the inflow cells 16 through the openings of the inflow cells 16 on the first end surface 13 of the honeycomb carrier 12 .

The ammonia gas flowing into the inflow cell 16 flows out to the outflow cell 17 through the ATR catalyst layer 26 and the partition wall 18 . The ATR catalyst layer 26 burns part of the ammonia gas passing through the ATR catalyst layer 26, and reforms the remaining ammonia gas passing through the ATR catalyst layer 26 with the heat generated by the combustion of the ammonia gas. Therefore, the reformed gas flows into the outflow cells 17 and the reformed gas flows out from the outflow cells 17 . Although the ammonia gas passes through the partition wall 18 , the pressure loss of the ammonia gas due to the partition wall 18 is high. Therefore, the ammonia gas that has spread throughout the space of the inflow cell 16 uniformly passes through the partition wall 18 without bias.

Since the ammonia gas uniformly passes through the partition wall 18 without bias, the combustion reaction is not excessively biased in the longitudinal direction from the first end face 13 to the second end face 14 of the honeycomb carrier 12 . That is, the combustion reaction is less likely to be biased in the longitudinal direction of the honeycomb carrier 12 . Specifically, as shown by the solid line graph in FIG. 5, in the present embodiment, the temperature difference between the upstream and downstream sides of the honeycomb carrier 12 in the ammonia gas reforming device 11 is suppressed. The dotted line graph in FIG. 5 shows a comparative example using a flow-through type honeycomb carrier. The temperature difference in this embodiment is smaller than in the comparative example.

In addition, since the reforming of ammonia gas by the ATR catalyst is an endothermic reaction, the reforming efficiency decreases when the temperature of the ammonia gas decreases. As shown in the graph of FIG. 5, if the lower limit temperature at which ammonia gas is efficiently reformed is T1, and the upper limit temperature at which the honeycomb carrier 12 is not damaged or deteriorated is T2, then the ammonia gas reforming apparatus of the present embodiment is 11 becomes equal to or higher than T1 and equal to or lower than T2. Incidentally, in the comparative example, since the honeycomb carrier 12 is of the flow-through type, the fuel gas passes through the cell space from the inlet toward the outlet, and the combustion reaction concentrates on the upstream side of the honeycomb carrier. Therefore, the temperature becomes T2 or higher upstream of the honeycomb carrier of the comparative example, and the honeycomb carrier 12 may be damaged or deteriorated. In addition, since the temperature is T1 or lower downstream of the honeycomb carrier of the comparative example, the reforming efficiency of the ammonia gas is lowered.

The ammonia gas reformer 11 according to this embodiment has the following effects.
(1) After the ammonia gas flows into the inflow cell 16 , it passes through the partition wall 18 and flows out to the outflow cell 17 . By arranging the inflow cell 16 , the partition wall 18 and the outflow cell 17 , the portion through which the ammonia gas passes is less likely to be biased within the partition wall 18 . This is because the partition wall 18 has a high pressure loss, so that the ammonia gas spreads throughout the entire space of the inflow cell 16 and then uses almost the entire partition wall 18 to pass through. The partition wall 18 carries an ATR catalyst as an ATR catalyst layer 26 . Since the location where the fuel gas passes through the partition wall 18 is less likely to be biased, the temperature difference in the partition wall 18 can be made as small as possible. As a result, damage and deterioration of the ammonia gas reforming device 11 can be prevented, and the efficiency of reforming ammonia by the ATR catalyst can be improved.

(2) The partition wall 18 has an inflow cell side wall portion 22 facing the inflow cell 16 and an outflow cell side wall portion 24 facing the outflow cell 17, and the ATR catalyst as the ATR catalyst layer 26 is provided on the inflow cell side wall portion 22 Carried. Therefore, even if an ATR catalyst that may be peeled off is used in the ATR catalyst layer 26 on the inflow cell 16 side, the peeled ATR catalyst powder stays in the inflow cell 16 and does not flow out to the outflow cell 17 . Therefore, the peeled powder of the ATR catalyst does not adversely affect the reformed gas utilization device existing downstream of the ammonia gas reforming device 11 .

(Second embodiment)
Next, an ammonia gas reforming apparatus according to a second embodiment will be described. This embodiment is an example in which an ATR catalyst layer is supported in the inflow cells of the honeycomb carrier. The ATR catalyst layer is formed by stacking a combustion catalyst on a reforming catalyst layer supported on the side walls of the inflow cells. It is different from the first embodiment in this point. In this embodiment, the description of the first embodiment is used for the same configuration as that of the first embodiment, and common reference numerals are used.

As shown in FIGS. 6( a ) and 6 ( b ), in the ammonia gas reformer 31 according to the present embodiment, the ATR catalyst layer 32 is carried on the inflow cell side wall portion 22 of the honeycomb carrier 12 . The ATR catalyst layer 32 has a reforming catalyst layer 34 supported on the inflow cell side wall portion 22 and a combustion catalyst layer 33 supported so as to cover the reforming catalyst layer 34 . That is, the ATR catalyst layer 32 has a laminated structure in which the combustion catalyst layer 33 and the reforming catalyst layer 34 are not mixed but are laminated together.

In this embodiment, the ammonia gas supplied to the honeycomb carrier 12 flows into the inflow cells 16 through the openings of the inflow cells 16 on the first end surface 13 of the honeycomb carrier 12 . Ammonia gas that has flowed into the inflow cell 16 passes through the combustion catalyst layer 33 on the surface side of the ATR catalyst layer 32, passes through the reforming catalyst layer 34 on the partition wall 18 side, and then passes through the partition wall 18 to the outflow cell 17. leak. The combustion catalyst layer 33 burns a portion of the ammonia gas passing through the combustion catalyst layer 33, and the reforming catalyst layer 34 reforms the ammonia gas passing through the reforming catalyst with the heat generated by the combustion of the ammonia gas.

In this embodiment, in the ATR catalyst layer 32 carried on the inflow cell side wall portion 22, the combustion catalyst layer 33 is laminated on the reforming catalyst layer 34, so the catalytic function of the ATR catalyst can be separated. . For example, by individually adjusting the amounts of the combustion catalyst and the reforming catalyst, it becomes easier to control the reaction as the ATR catalyst. Further, since the ammonia gas passes through the combustion catalyst layer 33 and then through the reforming catalyst layer 34, it is easy to secure the heat necessary for reforming ammonia by combustion. Furthermore, since the ATR catalyst is not carried on the outflow cell side walls 24 , even if the ATR catalyst which may be peeled off is used, peeled powder will not be sent to the downstream side of the honeycomb carrier 12 .

(Third embodiment)
Next, an ammonia gas reforming apparatus according to a third embodiment will be described. This embodiment differs from the first embodiment in that the ATR catalyst is supported not only on the inflow cell side but also on the outflow cell side of the honeycomb carrier. In this embodiment, the description of the first embodiment is used for the same configuration as that of the first embodiment, and common reference numerals are used.

As shown in FIGS. 7(a) and 7(b), in the ammonia gas reformer 41 according to the present embodiment, the ATR catalyst layer 26 is supported on the inflow cell side wall portion 22 of the honeycomb carrier 12. , the ATR catalyst layer 42 is supported on the outflow cell side wall portion 24 . The ATR catalyst layer 26 supported on the inflow cell side wall portion 22 and the ATR catalyst layer 42 supported on the outflow cell side wall portion 24 are composed of catalysts having the same composition.

In this embodiment, the ammonia gas supplied to the honeycomb carrier 12 flows into the inflow cells 16 through the openings of the inflow cells 16 on the first end surface 13 of the honeycomb carrier 12 . The ammonia gas flowing into the inflow cell 16 flows out to the outflow cell 17 through the ATR catalyst layer 26 , the partition wall 18 and the ATR catalyst layer 32 . The ATR catalyst layers 26, 42 burn part of the ammonia gas passing through the ATR catalyst layers 26, 42, and reform the remaining ammonia gas with heat from the combustion of the ammonia gas.

The ammonia gas reforming device 41 of the present embodiment has the same effect as that of the first embodiment in uniformizing the temperature in the honeycomb carrier 12 . Furthermore, in the ammonia gas reformer 41 of the present embodiment, the ATR catalyst layer 26 is supported on the inflow cell side wall portion 22, and the ATR catalyst layer 42 is supported on the outflow cell side wall portion 24. Therefore, the first The amount of ATR catalyst in the honeycomb carrier 12 can be increased compared to the embodiment. Therefore, compared with the first embodiment, the reforming efficiency of ammonia can be improved.

In this embodiment, the ATR catalyst layers 26 and 42 have the same composition, but the ATR catalyst layers 26 and 42 may have different compositions. For example, the material of the ATR catalyst layer 26 of the inflow cell side wall portion 22 is a catalyst having a composition containing at least one of cobalt-based catalyst, rhodium-based catalyst, ruthenium-based catalyst, and palladium-based catalyst. On the other hand, the ATR catalyst layer 42 of the outflow cell side wall portion 24 includes at least one of a cobalt-based catalyst, a rhodium-based catalyst, a ruthenium-based catalyst, and a palladium-based catalyst, and the ATR catalyst layer of the inflow cell side wall portion 22 is Any material different from 26 may be used. In this case, since appropriate catalysts can be selected for each of the ATR catalyst layer 26 on the inflow cell 16 side and the ATR catalyst layer 42 on the outflow cell 17 side, the ammonia reforming efficiency can be improved. .

(Fourth embodiment)
Next, an ammonia gas reforming apparatus according to a fourth embodiment will be described. This embodiment differs from the first embodiment in that the combustion catalyst is carried on the inflow cell side of the honeycomb carrier and the reforming catalyst is carried on the outflow cell side of the honeycomb carrier. In this embodiment, the description of the first embodiment is used for the same configuration as that of the first embodiment, and common reference numerals are used.

As shown in FIGS. 8(a) and 8(b), in the ammonia gas reformer 51 according to the present embodiment, a combustion catalyst layer 52 is carried on the inflow cell side wall portion 22 of the honeycomb carrier 12. , a reforming catalyst layer 53 is supported on the outflow cell side wall portion 24 . The combustion catalyst of the combustion catalyst layer 52 and the reforming catalyst of the reforming catalyst layer 53 are the same as the combustion catalyst and reforming catalyst of the first embodiment.

In this embodiment, the ammonia gas supplied to the honeycomb carrier 12 flows into the inflow cells 16 through the openings of the inflow cells 16 on the first end surface 13 of the honeycomb carrier 12 . The ammonia gas flowing into the inflow cell 16 flows out to the outflow cell 17 through the combustion catalyst layer 52 , the partition wall 18 and the reforming catalyst layer 53 . The combustion catalyst layer 52 burns part of the passing ammonia gas, and the reforming catalyst layer 53 reforms the remaining passing ammonia gas with the heat generated by the combustion of the ammonia gas.

In this embodiment, the combustion catalyst contained in the ATR catalyst is carried as the combustion catalyst layer 52 on the inflow cell side wall portion 22, and the reforming catalyst contained in the ATR catalyst is carried as the reforming catalyst layer 53 in the outflow cell side wall portion 24. Therefore, the catalytic function of the ATR catalyst can be separated. For example, by individually adjusting the amounts of the combustion catalyst and the reforming catalyst, it becomes easier to control the reaction as the ATR catalyst. In addition, in the present embodiment, heat required for reforming the fuel gas can be easily obtained in the inflow cell 16, so that the reforming efficiency of the ammonia gas by the reforming catalyst layer 53 in the outflow cell 17 can be improved.

(Fifth embodiment)
Next, the ammonia gas reformer according to this embodiment will be described. The ammonia gas reformer of this embodiment differs from the first embodiment in that the ATR catalyst is supported on the inflow cell side wall and the interior of the partition wall excluding the inflow cell side wall. In this embodiment, the description of the first embodiment is used for the same configuration as that of the first embodiment, and common reference numerals are used.

As shown in FIGS. 9A and 9B, in the ammonia reformer 61 according to the present embodiment, the ATR catalyst layer 26 is supported on the inflow cell side wall portion 22, and the inflow cell side wall portion of the partition wall 18 is supported. ATR catalyst is impregnated in the parts except the part 22 . That is, the inner wall portion 25 as the inside of the partition wall 18 is impregnated with the ATR catalyst. In FIG. 9B , the portion of the partition wall 18 impregnated with the ATR catalyst is referred to as the catalyst impregnated portion 62 , and the portion of the partition wall 18 not impregnated with the ATR catalyst is referred to as the non-catalyst impregnated portion 63 . In this embodiment, part of the inner wall portion 25 is the non-catalyst-impregnated portion 63 and the rest is the catalyst-impregnated portion 62 .

In this embodiment, the ammonia gas supplied to the honeycomb carrier 12 flows into the inflow cells 16 through the openings of the inflow cells 16 on the first end surface 13 of the honeycomb carrier 12 . The ammonia gas flowing into the inflow cell 16 flows out to the outflow cell 17 through the ATR catalyst layer 26 and the partition walls 18 . The ATR catalyst in the catalyst-impregnated portion 72 burns part of the ammonia gas passing through the partition wall 18 and reforms the remaining ammonia gas with the heat generated by the combustion of the ammonia gas.

According to the present embodiment, an effect equivalent to that of the first embodiment can be obtained in uniformizing the temperature of the honeycomb carrier 12 . Furthermore, according to the ammonia reformer 61 of this embodiment, the ammonia gas passing through the partition wall 18 can be burned and reformed. In addition, by impregnating the partition walls 18 with the ATR catalyst, the amount of the ATR catalyst can be increased compared to the first embodiment, so that the reforming efficiency of the ammonia gas can be further improved. Furthermore, since no ATR catalyst layer is provided on the outflow cell side, the amount of ATR catalyst in the honeycomb carrier 12 can be increased without causing peeling powder of the ATR catalyst.

In the present embodiment, part of the inner wall portion 25 is the non-catalyst-impregnated portion 63 and the rest is the catalyst-impregnated portion 62 , but the present invention is not limited to this. For example, all of the partition walls 18 may be impregnated with the ATR catalyst. Also, an ATR catalyst layer 26 may be provided on the outflow cell side wall portion 24 .

It should be noted that the above embodiment shows one embodiment of the present invention, and the present invention is not limited to the above embodiment, and various modifications can be made within the scope of the invention as described below. It is possible.

(circle) said embodiment illustrated and demonstrated ammonia gas as fuel gas, However, It does not restrict to this. The fuel gas may be ammonia gas or hydrocarbon-based gas such as methane. In this case, an ATR catalyst suitable for reforming hydrocarbon gas should be selected.

11, 31, 41, 51, 61 ammonia gas reformer 12 honeycomb carrier 13 first end face 14 second end face 15 outer peripheral wall 16 inflow cell 17 outflow cell 18 partition wall 19 outflow plug 20 inflow plug 21 surface 22 inflow cell side wall 23 surface 24 outlet cell side wall 25 inner wall 26, 32, 42 ATR catalyst layers 33, 52 combustion catalyst layers 34, 53 reforming catalyst layer 62 catalyst impregnated portion 63 catalyst non-impregnated portion F arrow (flow of ammonia gas)

Claims (7)

an inflow cell with an open upstream end and a plugged downstream end; an outflow cell with an open downstream end and a plugged upstream end; a porous honeycomb carrier having partition walls partitioning the cells and the outflow cells;
A fuel gas reforming device supported on the honeycomb carrier and including an ATR catalyst for reforming fuel gas,
A fuel gas reformer, wherein the ATR catalyst is supported on the partition wall. The partition is
an inflow cell sidewall facing the inflow cell;
an outflow cell sidewall facing the outflow cell,
2. A fuel gas reforming apparatus according to claim 1, wherein said ATR catalyst is supported on said inflow cell sidewall. 3. A fuel gas reformer according to claim 2, wherein said ATR catalyst is supported on said outflow cell side wall. The ATR catalyst has a combustion catalyst,
4. The fuel gas reforming apparatus according to claim 2, wherein the combustion catalyst is supported on the side walls of the inflow cells. 4. A fuel gas reformer according to claim 3, wherein the material of said ATR catalyst carried on said inflow cell side walls is different from the material of said ATR catalyst carried on said outflow cell side walls. The fuel gas reformer according to any one of claims 2 to 5, wherein the ATR catalyst is supported on the inflow cell side wall portion and the interior of the partition wall excluding the inflow cell side wall portion. quality equipment. The ATR catalyst has a combustion catalyst that burns fuel gas,
7. The fuel gas reforming apparatus according to claim 6, wherein the combustion catalyst is supported only on the side walls of the inflow cells.

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