Fuel Gas Reformer

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

[Technical Field]

[0001] The present invention relates to a fuel gas reformer. [Background technology]

[0002] A conventional fuel gas reformer is known, for example, from the technology described in Patent Document 1. The reformer described in Patent Document 1 is a device that supplies ammonia and an oxygen-containing gas and generates hydrogen through a reforming reaction. The reformer uses a honeycomb catalyst that promotes the autothermal reforming (ATR) reaction.

[0003] Furthermore, Patent Document 2 describes an ammonia reforming catalyst. In Patent Document 2, ammonia and an oxygen-containing gas pass through a reactor carrying the ammonia reforming catalyst from the inlet to the outlet, and a combustion reaction is likely to occur near the inlet. As a result, the temperature near the inlet is about 200°C higher than near the outlet. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Japanese Patent Application Laid-Open No. 2015-188820 [Patent Document 2] Japanese Patent Application Laid-Open No. 2010-214225 Summary of the Invention [Problem to be solved by the invention]

[0005] The technology described in Patent Document 2 aims to control the temperature rise of the catalyst layer and prevent damage to the reformer and catalyst degradation, but there is a problem in that a temperature difference of about 200°C still occurs in the reformer, making it impossible to fully prevent damage and degradation of the reformer. Lowering the temperature of the reformer could be considered to solve the above problem, but in this case, the temperature near the outlet of the reactor would be low, resulting in a deterioration in reforming efficiency. The technology disclosed in Patent Document 1 does not mention anything about preventing damage and degradation of the reformer caused by temperature differences.

[0006] 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 that can minimize the temperature difference caused by the reaction in the honeycomb support. [Means for solving the problem]

[0007] In order to solve the above problems, the present invention provides a porous honeycomb support having inlet cells that are open at their upstream ends and plugged at their downstream ends, outlet cells that are open at their downstream ends and plugged at their upstream ends, and partition walls that separate the inlet cells and the outlet cells; A combustion catalyst for burning fuel gas and Fuel gas To hydrogen to reform Contains reforming catalyst In a fuel gas reforming apparatus including an ATR catalyst, the partition wall has an inflow cell side wall portion facing the inflow cell, an outflow cell side wall portion facing the outflow cell, and an inner wall portion sandwiched between the inflow cell side wall portion and the outflow cell side wall portion; the ATR catalyst is provided on the inlet cell side wall portion ATR catalyst layer supported on the surface of and, a first catalyst-impregnated portion impregnated in the inlet cell side wall portion and a second catalyst-impregnated portion impregnated in the inner wall portion, before Recording Output cell side wall part is characterized in that a catalyst non-impregnated portion is provided.

[0008] In such a reformer, fuel gas flows into the inlet cells, passes through the partition walls, and flows out into the outlet cells. By arranging the inlet cells, partition walls, and outlet cells, the fuel gas is less likely to pass through unevenly within the partition walls. This is because the pressure loss through the partition walls is high, so the fuel gas spreads throughout the entire space of the inlet cells and then passes through almost the entire partition walls. An ATR catalyst is supported on the partition walls. By preventing the fuel gas from passing through unevenly, the temperature difference in the partition walls can be minimized.

[0009] Also 、A Since the TR catalyst is supported on the side wall of the inlet cell, even if an ATR catalyst, which may peel off, is used, the peeled powder will not flow into the outlet cell.

[0013] Also , interval The ATR catalyst is supported inside the wall, and the amount of ATR catalyst can be further increased, thereby further improving the reforming efficiency. [Effects of the Invention]

[0015] According to the present invention, it is possible to provide a fuel gas reforming device that can minimize the temperature difference caused by the reaction in the honeycomb support. [Brief explanation of the drawings]

[0016] [Figure 1] 1 is a perspective view schematically showing an ammonia gas reforming apparatus according to a first embodiment. [Figure 2] FIG. 2 is a front view showing the upstream end of the ammonia gas reformer. [Figure 3] FIG. 3 is a view taken along the line AA in FIG. 2. [Figure 4] 4(a) is an enlarged view of FIG. 2, and FIG. 4(b) is a view taken along the line AA in FIG. 4(a). [Figure 5] 1 is a graph showing the change in temperature from the inlet side to the outlet side of the ammonia gas reformer. [Figure 6]6(a) is a cross-sectional view showing a layer structure according to the second embodiment, and FIG. 6(b) is a view taken along the line CC in FIG. 6(a). [Figure 7] 7(a) is a cross-sectional view showing a layer structure according to the third embodiment, and FIG. 7(b) is a view taken along the line DD in FIG. 7(a). [Figure 8] 8(a) is a cross-sectional view showing a layer structure according to a fourth embodiment, and FIG. 8(b) is a view taken along the arrow EE in FIG. 8(a). [Figure 9] 9(a) is a cross-sectional view showing a layer structure according to the fifth embodiment, and FIG. 9(b) is a view taken along the line GG in FIG. 9(a). DETAILED DESCRIPTION OF THE INVENTION

[0017] (First embodiment) A first embodiment of the present invention will be described below with reference to the drawings. In this embodiment, an ammonia gas reformer will be described as a fuel gas reformer that uses ammonia gas as fuel gas.

[0018] 1, an ammonia gas reforming apparatus 11 of this embodiment has a honeycomb support 12 formed of porous ceramic having a honeycomb structure. The honeycomb support 12 has a first end face 13 which is one end face, a second end face 14 which is the other end face, and a cylindrical outer peripheral wall 15.

[0019] As shown in Figures 1 and 2, the honeycomb support body 12 has a plurality of inlet cells 16, a plurality of outlet cells 17, and partition walls 18. As shown in Figure 3, the inlet cells 16 are disposed inside the outer peripheral wall 15 and extend from the first end face 13 to the second end face 14, with the openings of the second end face 14 being plugged with outlet plugs 19. The outlet cells 17 are adjacent to the inlet cells 16 and extend from the first end face 13 to the second end face 14, with the openings of the first end face 13 being plugged with inlet plugs 20.

[0020] The partition walls 18 define a plurality of inlet cells 16 and outlet cells 17. The plurality of inlet cells 16 and outlet cells 17 are arranged in a lattice pattern by being defined by the partition walls 18. Therefore, as shown in FIG. 2, the inlet cells 16 and outlet cells 17 are alternately arranged in a checkerboard pattern on the first end face 13. The partition walls 18 are surrounded by the cylindrical outer wall 15, so that the honeycomb support 12 is formed in a cylindrical shape. The honeycomb support 12 of this embodiment is a wall-flow type honeycomb support in which a fluid flows from the inlet cells 16 to the outlet cells 17. In FIG. 3, the flow of ammonia gas is indicated by arrow F.

[0021] As shown in FIG. 4, the partition wall 18 has an inlet cell side wall portion 22 including a surface 21 on the inlet cell 16 side, an outlet cell side wall portion 24 including a surface 23 on the outlet cell 17 side, and an inner wall portion 25 excluding the inlet cell side wall portion 22 and the outlet cell side wall portion 24.

[0022] The honeycomb support 12 of this embodiment is formed of porous ceramics. However, other ceramics with excellent heat resistance, such as cordierite, mullite, and silicon nitride, may also be used, or a combination of multiple ceramics may be used. The material of the honeycomb support 12 preferably contains at least one selected from the group consisting of cordierite, silicon carbide, silicon nitride, and mullite. More specifically, the material preferably contains 20% by mass or more, more preferably 30% by mass or more, and particularly preferably 50% by mass or more of a material listed in this group. The honeycomb support 12 is obtained by extruding a ceramic material kneaded with water and a binder using an extruder, cutting and drying the extruded body, and firing it after drying.

[0023] The ammonia gas reformer 11 has a honeycomb support 12 and an ATR catalyst supported on the honeycomb support 12. The ATR catalyst is a catalyst that reforms ammonia gas in an autothermal reformer (ATR). The ATR catalyst burns ammonia gas in a temperature range of, for example, about 200°C to 400°C, and reforms the ammonia gas in a temperature range higher than the combustion temperature of ammonia gas (for example, about 250°C to 500°C). The ATR catalyst includes a combustion catalyst that burns ammonia gas and a reforming catalyst that reforms the ammonia gas into hydrogen. The catalytic metal of the combustion catalyst can be V, Cr, Mn, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, W, Re, Os, Ir, or Pt. In addition, the catalytic metal for the reforming catalyst can be V, Cr, Mn, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, W, Re, Os, Ir, or Pt.

[0024] As shown in Fig. 4, the ATR catalyst in this embodiment is supported as an ATR catalyst layer 26 on the inlet cell sidewall 22. The required amount of ATR catalyst is supported by applying a catalyst slurry to the inlet cell sidewall 22 using a washcoat method, removing excess ATR catalyst with air blowing, and drying the ATR catalyst at 120°C. The application and drying of the catalyst slurry is repeated. The honeycomb support 12 is then fired, and the ATR catalyst layer 26 is formed by performing a reduction treatment after firing.

[0025] In this embodiment, an ammonia supplier (not shown) for storing ammonia and an air supplier (not shown) for supplying air are disposed upstream of the ammonia gas reformer 11. In addition, a reformed gas utilization device (not shown) for utilizing the reformed gas reformed by the ammonia gas reformer 11 is provided downstream of the ammonia gas reformer 11. Therefore, ammonia gas obtained by mixing ammonia and air is supplied to the ammonia gas reformer 11, and the ammonia gas reformer 11 reforms the ammonia gas to generate a reformed gas. The generated reformed gas is utilized in the reformed gas utilization device.

[0026] Next, the reforming of ammonia gas by the ammonia gas reformer 11 according to this embodiment will be described. First, ammonia gas obtained by mixing 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 reformer 11 flows into the inlet cells 16 from the openings of the inlet cells 16 on the first end face 13 of the honeycomb support 12.

[0027] The ammonia gas that has flowed into the inlet cells 16 flows out into the outlet cells 17 through the ATR catalyst layer 26 and the partition walls 18. The ATR catalyst layer 26 combusts a portion of the ammonia gas that passes through the ATR catalyst layer 26, and reforms the remaining ammonia gas that passes through the ATR catalyst layer 26 with the heat from the combustion of the ammonia gas. Therefore, the reformed gas flows into the outlet cells 17 and flows out from the outlet cells 17. Although the ammonia gas passes through the partition walls 18, the pressure loss of the ammonia gas due to the partition walls 18 is high, so the ammonia gas passes through the entire space of the inlet cells 16 after spreading throughout the space before passing through the partition walls 18. Therefore, the ammonia gas that has spread throughout the entire space of the inlet cells 16 passes through the partition walls 18 evenly without any unevenness.

[0028] Because the ammonia gas passes through the partition walls 18 uniformly without bias, the combustion reaction does not become excessively biased in the length direction from the first end face 13 to the second end face 14 of the honeycomb support 12. In other words, the combustion reaction is less likely to become biased in the length direction of the honeycomb support 12. Specifically, as shown by the solid line graph in Figure 5, in this embodiment, the temperature difference between the upstream and downstream of the honeycomb support 12 in the ammonia gas reformer 11 is suppressed. Note that the dotted line graph in Figure 5 shows a comparative example using a flow-through type honeycomb support. The temperature difference in this embodiment is smaller than in the comparative example.

[0029] Furthermore, because the reforming of ammonia gas using an ATR catalyst is an endothermic reaction, a decrease in the temperature of the ammonia gas reduces the reforming efficiency. As shown in the graph of FIG. 5, if T1 is the lower limit temperature at which ammonia gas is efficiently reformed and T2 is the upper limit temperature at which the honeycomb support 12 is not damaged or deteriorated, the temperature in the ammonia gas reformer 11 of this embodiment is above T1 and below T2. Incidentally, in the comparative example, since the honeycomb support 12 is a flow-through type, the fuel gas passes through the cell space from the inlet to the outlet, and the combustion reaction is concentrated on the upstream side of the honeycomb support. Therefore, the temperature upstream of the honeycomb support of the comparative example exceeds T2, which may damage or deteriorate the honeycomb support 12. Furthermore, the temperature downstream of the honeycomb support of the comparative example is below T1, which reduces the reforming efficiency of the ammonia gas.

[0030] The ammonia gas reforming device 11 according to this embodiment has the following advantages. (1) Ammonia gas flows into the inlet cells 16, passes through the partition walls 18, and flows out into the outlet cells 17. By arranging the inlet cells 16, the partition walls 18, and the outlet cells 17, the ammonia gas is less likely to pass through unevenly within the partition walls 18. This is because the pressure loss through the partition walls 18 is high, so the ammonia gas spreads throughout the entire space of the inlet cells 16 and then passes through almost the entire partition walls 18. The partition walls 18 support an ATR catalyst as the ATR catalyst layer 26. Since the fuel gas is less likely to pass unevenly through the partition walls 18, the temperature difference in the partition walls 18 can be minimized. As a result, damage and deterioration of the ammonia gas reformer 11 can be prevented, and the efficiency of ammonia reforming by the ATR catalyst can be improved.

[0031] (2) The partition wall 18 has an inlet cell side wall 22 facing the inlet cell 16 and an outlet cell side wall 24 facing the outlet cell 17, and the ATR catalyst as the ATR catalyst layer 26 is supported on the inlet cell side wall 22. Therefore, even if an ATR catalyst that may peel off is used in the ATR catalyst layer 26 on the inlet cell 16 side, the peeled powder of the peeled ATR catalyst remains in the inlet cell 16 and does not flow out to the outlet cell 17. Therefore, the peeled powder of the ATR catalyst does not adversely affect the reformed gas utilization device located downstream of the ammonia gas reformer 11.

[0032] (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 inlet cells of a honeycomb support, but differs from the first embodiment in that the ATR catalyst layer is a reforming catalyst layer supported on the side walls of the inlet cells, on which a combustion catalyst is laminated. In this embodiment, the same components as those in the first embodiment will be referred to and the same reference numerals will be used.

[0033] 6(a) and 6(b), in an ammonia gas reformer 31 according to this embodiment, an ATR catalyst layer 32 is supported on the inlet cell side wall portion 22 of the honeycomb support 12. The ATR catalyst layer 32 has a reforming catalyst layer 34 supported on the inlet cell side wall portion 22, and a combustion catalyst layer 33 supported so as to cover the reforming catalyst layer 34. In other words, the ATR catalyst layer 32 has a layered structure in which the combustion catalyst layer 33 and the reforming catalyst layer 34 are not mixed but are stacked on top of each other.

[0034] In this embodiment, ammonia gas supplied to the honeycomb support 12 flows into the inlet cells 16 from the openings of the inlet cells 16 in the first end face 13 of the honeycomb support 12. The ammonia gas that has flowed into the inlet cells 16 passes through the combustion catalyst layer 33 on the surface side of the ATR catalyst layer 32, then passes through the reforming catalyst layer 34 on the partition wall 18 side, and further flows out to the outlet cells 17 through the partition wall 18. The combustion catalyst layer 33 combusts 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 by the heat generated by the combustion of the ammonia gas.

[0035] In this embodiment, the ATR catalyst layer 32 supported on the inlet cell sidewall 22 has the combustion catalyst layer 33 laminated on the reforming catalyst layer 34, allowing the catalytic functions of the ATR catalyst to be separated. For example, the reaction of the ATR catalyst can be easily controlled by separately adjusting the amounts of the combustion catalyst and reforming catalyst. Furthermore, because ammonia gas passes through the combustion catalyst layer 33 before passing through the reforming catalyst layer 34, the heat required for reforming ammonia can be easily obtained through combustion. Furthermore, because the ATR catalyst is not supported on the outlet cell sidewall 24, even if an ATR catalyst that may peel off is used, peeled powder will not be sent downstream of the honeycomb support 12.

[0036] (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 on the honeycomb support body not only on the inlet cell side but also on the outlet cell side. In this embodiment, the same configuration as in the first embodiment will be referred to and the same reference numerals will be used.

[0037] 7(a) and 7(b), in an ammonia gas reforming apparatus 41 according to this embodiment, an ATR catalyst layer 26 is supported on the inlet cell side wall portions 22 of the honeycomb support 12, and an ATR catalyst layer 42 is supported on the outflow cell side wall portions 24. The ATR catalyst layer 26 supported on the inlet cell side wall portions 22 and the ATR catalyst layer 42 supported on the outflow cell side wall portions 24 are made of catalysts having the same composition.

[0038] In this embodiment, ammonia gas supplied to the honeycomb support 12 flows into the inlet cells 16 from the openings of the inlet cells 16 in the first end face 13 of the honeycomb support 12. The ammonia gas that has flowed into the inlet cells 16 flows through the ATR catalyst layer 26, the partition walls 18, and the ATR catalyst layer 32 and flows out to the outlet cells 17. The ATR catalyst layers 26, 42 combust a portion of the ammonia gas passing through the ATR catalyst layers 26, 42, and reform the remaining ammonia gas with the heat generated by the combustion of the ammonia gas.

[0039] The ammonia gas reforming apparatus 41 of this embodiment has the same effect as the first embodiment in terms of temperature uniformity in the honeycomb support 12. Furthermore, the ammonia gas reforming apparatus 41 of this embodiment has the ATR catalyst layer 26 supported on the inlet cell side wall portion 22 and the ATR catalyst layer 42 supported on the outlet cell side wall portion 24, so that the amount of ATR catalyst in the honeycomb support 12 can be increased compared to the first embodiment. Therefore, the ammonia reforming efficiency can be improved compared to the first embodiment.

[0040] In this embodiment, the ATR catalyst layers 26, 42 have the same catalyst composition. However, the ATR catalyst layers 26, 42 may have different catalyst compositions. For example, the ATR catalyst layer 26 on the inlet cell sidewall 22 may be made of a catalyst containing at least one of a cobalt-based catalyst, a rhodium-based catalyst, a ruthenium-based catalyst, and a palladium-based catalyst. On the other hand, the ATR catalyst layer 42 on the outlet cell sidewall 24 may be made of a different material than the ATR catalyst layer 26 on the inlet cell sidewall 22. In this case, appropriate catalysts can be selected for the ATR catalyst layer 26 on the inlet cell 16 side and the ATR catalyst layer 42 on the outlet cell 17 side, thereby improving the ammonia reforming efficiency.

[0041] (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 a combustion catalyst is supported on the inlet cell side of the honeycomb support, and a reforming catalyst is supported on the outlet cell side. In this embodiment, the same configuration as in the first embodiment will be referred to and the same reference numerals will be used.

[0042] As shown in Figures 8(a) and 8(b), in an ammonia gas reformer 51 according to this embodiment, a combustion catalyst layer 52 is supported on the inlet cell side wall portion 22 of a honeycomb support 12, and a reforming catalyst layer 53 is supported on the outlet 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.

[0043] In this embodiment, ammonia gas supplied to the honeycomb support 12 flows into the inlet cells 16 from the openings of the inlet cells 16 in the first end face 13 of the honeycomb support 12. The ammonia gas that has flowed into the inlet cells 16 flows through the combustion catalyst layer 52, the partition walls 18, and the reforming catalyst layer 53 to the outlet cells 17. The combustion catalyst layer 52 combusts a portion of the ammonia gas that passes through, and the reforming catalyst layer 53 reforms the remaining ammonia gas that passes through with the heat generated by the combustion of the ammonia gas.

[0044] In this embodiment, the combustion catalyst included in the ATR catalyst is supported on the inlet cell sidewall 22 as the combustion catalyst layer 52, and the reforming catalyst included in the ATR catalyst is supported on the outlet cell sidewall 24 as the reforming catalyst layer 53, so the catalytic functions of the ATR catalyst can be separated. For example, the reaction as an ATR catalyst can be easily controlled by separately adjusting the amounts of the combustion catalyst and the reforming catalyst. Furthermore, in this embodiment, the heat required for reforming the fuel gas can be easily obtained in the inlet cell 16, so the efficiency of reforming ammonia gas by the reforming catalyst layer 53 in the outlet cell 17 can be improved.

[0045] (Fifth embodiment) Next, an ammonia gas reforming apparatus according to this embodiment will be described. The ammonia gas reforming apparatus of this embodiment differs from the first embodiment in that the ATR catalyst is supported on the inlet cell side wall portions and the interior of the partition wall excluding the inlet cell side wall portions. In this embodiment, the same configuration as in the first embodiment will be referred to and the same reference numerals will be used.

[0046] As shown in Figures 9(a) and 9(b), in an ammonia reformer 61 according to this embodiment, the ATR catalyst layer 26 is supported on the inlet cell side wall portions 22, and the ATR catalyst is impregnated in the portions of the partition walls 18 excluding the inlet cell side wall portions 22. That is, the ATR catalyst is impregnated in the inner wall portions 25, which form the insides of the partition walls 18. In Figure 9(b), the portions of the partition walls 18 impregnated with the ATR catalyst are referred to as catalyst-impregnated portions 62, and the portions of the partition walls 18 that are not impregnated with the ATR catalyst are referred to as catalyst-non-impregnated portions 63. In this embodiment, a part of the inner wall portions 25 is the catalyst-non-impregnated portion 63, and the remainder is the catalyst-impregnated portion 62.

[0047] In this embodiment, the ammonia gas supplied to the honeycomb support 12 flows into the inlet cells 16 from the openings of the inlet cells 16 in the first end face 13 of the honeycomb support 12. The ammonia gas that has flowed into the inlet cells 16 flows out to the outlet cells 17 through the ATR catalyst layer 26 and the partition walls 18. The ATR catalyst in the catalyst-impregnated portion 72 combusts a portion of the ammonia gas that passes through the partition walls 18, and reforms the remaining ammonia gas with the heat generated by the combustion of the ammonia gas.

[0048] According to the present embodiment, the same effect as that of the first embodiment can be achieved in terms of temperature uniformity in the honeycomb support 12. Furthermore, according to the ammonia reformer 61 of the present embodiment, the ammonia gas passing through the partition walls 18 can be combusted and reformed. Furthermore, by impregnating the partition walls 18 with the ATR catalyst, the amount of the ATR catalyst can be increased compared to the first embodiment, and therefore the efficiency of reforming the ammonia gas can be further improved. Furthermore, since an ATR catalyst layer is not provided on the outflow cell side, the amount of the ATR catalyst in the honeycomb support 12 can be increased without generating peeled powder of the ATR catalyst.

[0049] In the present embodiment, a part of the inner wall portion 25 is the catalyst non-impregnated portion 63, and the remainder is the catalyst impregnated portion 62, but this is not limiting. For example, the entire partition wall 18 may be impregnated with the ATR catalyst. Also, the ATR catalyst layer 26 may be provided on the outflow cell side wall portion 24.

[0050] The above embodiment shows one embodiment of the present invention, and the present invention is not limited to the above embodiment, and various modifications are possible within the scope of the spirit of the invention as described below.

[0051] In the above embodiment, ammonia gas is used as the fuel gas, but the fuel gas is not limited to this. The fuel gas may be a hydrocarbon gas such as methane, in addition to ammonia gas. In this case, an ATR catalyst suitable for reforming the hydrocarbon gas may be selected. [Explanation of symbols]

[0052] 11, 31, 41, 51, 61 Ammonia gas reformer 12 Honeycomb carrier 13 First end surface 14 Second end face 15 Outer wall 16 inflow cells 17 Outflow Cell 18 Bulkhead 19 Outlet Plug 20 Inlet plug 21 Surface 22 Inlet cell side wall 23 Surface 24 Outflow cell side wall 25 Inner wall 26, 32, 42 ATR catalyst layer 33, 52 Combustion catalyst layer 34, 53 Reforming catalyst layer 62 Catalyst impregnation section 63 Catalyst non-impregnated section F Arrow (ammonia gas flow)

Claims

[Claim 1] a porous honeycomb support having inlet cells each having an open upstream end and a plugged downstream end, outlet cells each having an open downstream end and a plugged upstream end, and partition walls separating the inlet cells from the outlet cells; a fuel gas reforming apparatus including an ATR catalyst supported on the honeycomb support and including a combustion catalyst for burning fuel gas and a reforming catalyst for reforming the fuel gas into hydrogen, The partition wall is an inflow cell sidewall portion facing the inflow cell; an outflow cell sidewall portion facing the outflow cell; an inner wall portion sandwiched between the inflow cell side wall portion and the outflow cell side wall portion; the ATR catalyst comprises an ATR catalyst layer supported on the surface of the inlet cell side wall portion, a first catalyst-impregnated portion impregnated in the inlet cell side wall portion, and a second catalyst-impregnated portion impregnated in the inner wall portion, A fuel gas reforming apparatus, characterized in that a catalyst-unimpregnated portion is provided on the side wall of the outflow cell.

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