Reformer

Abstract

The utility model relates to a reformer which is provided with a catalyst container which comprises an interval in which a catalyst layer is formed and is configured to generate reformed gas through a reforming reaction accompanying heat absorption when raw material gas flowing in from one end surface of the catalyst layer passes through the catalyst layer, the reformed gas flows out from the other end surface of the catalyst layer; a plurality of reformed gas tubes which penetrate the catalyst layer and through which the reformed gas flows; and a heating device for heating the reformed gas in a section between the flow of the reformed gas out of the catalyst layer and the flow of the reformed gas into the plurality of reformed gas tubes. As a result, in the reformer that uses the catalyst to promote an endothermic reaction, i.e., a reforming reaction from the raw material gas to the reformed gas, the energy consumption of the heating device provided in the reformer can be reduced.

Description

Technical Field

[0001] The utility model relates to a reformer, in particular to a reformer for promoting the reforming reaction of raw gas. Background Art

[0002] Patent Document 1 discloses a catalytic ammonia decomposition device (so-called reformer). This device uses a catalyst to decompose ammonia into hydrogen and nitrogen. Generally, the decomposition efficiency of ammonia increases as the temperature increases. In addition, since the decomposition of ammonia is an endothermic reaction, heat energy is absorbed from the catalyst during the decomposition of ammonia. Therefore, in most cases, the reformer for decomposing ammonia is equipped with a heating device (heater) for heating ammonia and the catalyst.

[0003] Patent Document 1: Japanese Patent Application Publication No. 2019-131454 Utility Model Content

[0004] However, in the above-mentioned device, ammonia is injected through an ammonia supply pipe inserted into the inside of the catalyst layer composed of a catalyst and a structural material, and hydrogen and nitrogen generated by the decomposition of ammonia are captured at the periphery of the catalyst layer. Therefore, the ammonia passing through the ammonia supply pipe takes away the thermal energy of the catalyst layer and the ammonia inside it. In addition, the thermal energy of the catalyst layer is taken away with the decomposition reaction of ammonia (i.e., endothermic reaction). Therefore, the heating device that heats the catalyst layer is likely to consume a large amount of energy (e.g., electricity in the case of an electric heater).

[0005] In order to provide a reformer capable of reducing the energy consumption of a heating device, the technology disclosed in this specification adopts the following aspects.

[0006] The first embodiment of the utility model is a reformer, which comprises: a catalyst container, including a section where a catalyst layer is formed, configured to generate a reformed gas through a reforming reaction accompanied by heat absorption when a raw gas flowing in from one end face of the catalyst layer passes through the catalyst layer, and the reformed gas flows out from the other end face of the catalyst layer; a plurality of reforming gas pipes, which penetrate the catalyst layer and through which the reformed gas flows; and a heating device, which heats the reformed gas in a section after the reformed gas flows out of the catalyst layer until it flows into the plurality of reforming gas pipes.

[0007] According to a second aspect, in the reformer of the first aspect, inner diameters of the plurality of reformed gas pipes increase toward a downstream of the reformed gas in the catalyst layer.

[0008] The third embodiment of the present utility model is a reformer, which comprises: a catalyst container, including a section where a catalyst layer is formed, configured to generate a reformed gas through a reforming reaction accompanied by heat absorption when a raw gas flowing in from one end face of the catalyst layer passes through the catalyst layer, and the reformed gas flows out from the other end face of the catalyst layer; a heating device, which heats at least the catalyst layer; and a heat exchange part, which is used to exchange heat between the reformed gas and the raw gas before flowing into the catalyst layer.

[0009] The fourth mode is that, in the reformer of the third mode, there are: an outer raw gas flow path, which is configured in a manner that the raw gas flows outside the catalyst container; and an outer reforming gas flow path, which is configured in a manner that the reforming gas flows outside the outer raw gas flow path, the heating device is arranged on the outside of the catalyst layer and located on the inside of the outer raw gas flow path, heats the raw gas flowing in the catalyst layer and the outer raw gas flow path, and the heat exchange portion is composed of the outer reforming gas flow path and the outer raw gas flow path.

[0010] The fifth mode is that, in the reformer of the third mode, there are: a raw gas inlet path, configured to introduce the raw gas into the catalyst layer; and an inner reforming gas flow path, configured to penetrate the catalyst layer and allow the reforming gas to flow, the heating device is arranged on the outside of the catalyst layer, and the heat exchange part is composed of a section of the inner reforming gas flow path located downstream of the catalyst layer and the raw gas inlet path.

[0011] According to a sixth aspect, in the reformer of any one of the first to fifth aspects, the raw material gas is ammonia gas, and the reformed gas is a gas containing hydrogen gas and nitrogen gas generated by decomposition of the ammonia gas.

[0012] In the first mode, the reformed gas is heated by the heating device to a high temperature, and then the catalyst layer is heated by the high-temperature reformed gas circulating in a plurality of reformed gas pipes. That is, the portion of the catalyst layer heated from the inside (more specifically, the heat transfer area equal to the sum of the areas of the outer peripheral surfaces of the sections of the reformed gas pipes that penetrate the catalyst layer) increases as the number of reformed gas pipes increases. Therefore, most of the catalyst layer can be maintained at a temperature at which the catalyst is activated without heating a portion of the catalyst layer more than necessary. Therefore, according to the first mode, the possibility of excessive energy consumption of the heating device can be avoided.

[0013] However, the temperature of the reformed gas circulating in the reformed gas pipe decreases as it exchanges heat with the catalyst layer as it approaches the downstream. On the other hand, the reformed gas pipe in the second embodiment has a larger inner diameter at the downstream, so the flow rate of the reformed gas decreases. Therefore, compared with the case where the flow rate of the reformed gas is large, the heat transfer from the reformed gas to the catalyst is promoted. Therefore, it is possible to avoid as much as possible that the heat transfer to the catalyst layer decreases as the temperature of the reformed gas circulating in the reformed gas pipe decreases. Therefore, according to the second embodiment, it is possible to avoid excessive energy consumption of the heating device, and it is possible to increase the possibility of maintaining more parts of the catalyst layer at a temperature at which the catalyst is activated.

[0014] In the third embodiment, the reformed gas is at a relatively high temperature when it flows out of the catalyst layer heated by the heating device. Therefore, the raw gas flows into the catalyst layer after being heated by the reformed gas in the heat exchange section. Therefore, according to the third embodiment, the thermal energy of the reformed gas is effectively utilized, thereby avoiding the possibility of excessive energy consumption of the heating device.

[0015] In the fourth aspect, the raw gas flows into the catalyst layer after being heated by the heat exchanger and the heating device. Therefore, according to the fourth aspect, the possibility of avoiding excessive energy consumption of the heating device is further increased.

[0016] In the fifth embodiment, the reformed gas heats the catalyst layer (particularly the center of the catalyst layer far from the heating device) when circulating in the inner reformed gas flow path, and then heats the raw gas in the heat exchanger. According to the fifth embodiment, the possibility of avoiding excessive energy consumption of the heating device is further improved.

[0017] According to the sixth aspect, ammonia gas can be decomposed into hydrogen gas and nitrogen gas using the reformer. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 This is a block diagram of the fuel cell system according to the first embodiment.

[0019] Figure 2 It is a longitudinal cross-sectional view of the reformer according to the first embodiment.

[0020] Figure 3 This is a cross-sectional view of the reformer according to the first embodiment.

[0021] Figure 4 It is a longitudinal cross-sectional view of a reformer according to a modification of the first embodiment.

[0022] Figure 5 It is a longitudinal cross-sectional view of a reformer according to a second embodiment.

[0023] Figure 6 It is a longitudinal sectional view of a reformer according to a third embodiment.

[0024] Description of Reference Numerals

[0025] 1, 1a, 2, 3: reformer; 11: catalyst container; 11a: raw gas chamber; 11b: reforming gas chamber; 12: storage container; 13: insulation material; 14a, 14b: partition plate; 15: catalyst layer; 16: heater; 17: reforming gas flow path; 17a, 17b, 17c, 17d, 17e, 17f, 17g, 17h, 17i: reforming gas pipe; 18: reforming gas 19: reformed gas confluence; 21: reformed gas inflow pipe; 22: reformed gas outflow pipe; 23: raw gas inflow pipe; 24: reformed gas flow path; 24a, 24b, 24c, 24d: reformed gas pipe; 25: small diameter portion; 26: large diameter portion; 27: reformed gas branch; 28: reformed gas confluence; 31: catalyst container; 31a: catalyst container inflow port; 31b: raw gas inflow pipe : material gas chamber; 31c: reforming gas chamber; 32: intermediate container; 32a: outer raw gas flow path; 33: outer container; 33a: outer reforming gas flow path; 34: storage container; 35: insulation material; 36: catalyst container outflow pipe; 37a, 37b: dividing plate; 38: heater; 39: catalyst layer; 41: raw gas inflow pipe; 42: reforming gas outflow pipe; 51: catalyst container; 51a: raw gas chamber; 51b: reforming gas chamber; 52: storage container; 53: insulation material; 54a, 54b: dividing plate; 55: heater; 56: catalyst layer; 57: raw gas inflow path; 58: inner reforming gas flow path; 58a: catalyst layer penetration portion; 58b: reforming gas outflow portion; 91: ammonia storage; 92: adsorption device; 93: fuel cell; 100: fuel cell system. DETAILED DESCRIPTION

[0026] First Embodiment

[0027] Reference Figures 1 to 3 The first embodiment is described. The same reference numerals in the following description denote the same elements having the same functions, and the description thereof will not be repeated. A reformer 1 according to the first embodiment is applied to Figure 1 The fuel cell system 100 shown in FIG. The fuel cell system 100 includes an ammonia storage 91 , an adsorption device 92 , and a fuel cell 93 in addition to the reformer 1 .

[0028] Reformer

[0029] The reformer 1 promotes a reforming reaction in which ammonia (NH3) gas flowing in as a raw material gas from the ammonia storage 91 is decomposed into hydrogen (H2) and nitrogen (N2). The ammonia decomposition reaction is an endothermic reaction. The reformer 1 supplies a mixed gas containing hydrogen, nitrogen, and ammonia that does not participate in the reforming reaction to the adsorption device 92. That is, the main components of the mixed gas are reformed gas, i.e., hydrogen and nitrogen.

[0030] The ammonia storage 91 stores ammonia in a liquid state. The ammonia storage 91 is provided with a pump (not shown) for pressure-feeding a required amount of gasified ammonia (i.e., ammonia gas, raw gas) 1 to the reformer 1. The adsorption device 92 adsorbs ammonia contained in the mixed gas. The adsorption device 92 supplies the purified gas from which ammonia has been removed to the fuel cell 93. The fuel cell 93 generates electricity using hydrogen contained in the purified gas as fuel.

[0031] like Figure 2 As shown, the reformer 1 includes a catalyst container 11, a storage container 12, an insulating material 13, partition plates 14a, 14b, a catalyst layer 15, a heater 16, a reformed gas flow path 17, a reformed gas branching portion 18, a reformed gas converging portion 19, a reformed gas inlet pipe 21, a reformed gas outlet pipe 22 and a raw gas inlet pipe 23. Figure 3 As shown in FIG. 1 , the reformed gas flow path 17 is formed by a plurality of reformed gas pipes 17a, 17b, 17c, 17d, 17e, 17f, 17g, 17h, and 17i. Figure 2 The direction when observing.

[0032] Catalyst container

[0033] The catalyst container 11 and the storage container 12 are coaxially arranged and have Figure 2 The dot-dash line is a generally cylindrical shape with the axis L1. More specifically, the storage container 12 covers the catalyst container 11. The space formed between the inner wall surface of the storage container 12 and the outer wall surface of the catalyst container 11 is filled with a heat insulating material 13, which is a well-known heat insulating material.

[0034] The catalyst container 11 includes a raw gas chamber 11a, a catalyst layer 15, and a reformed gas chamber 11b inside. The catalyst layer 15 is adjacent to the raw gas chamber 11a above the raw gas chamber 11a. The reformed gas chamber 11b is adjacent to the catalyst layer 15 above the catalyst layer 15. The raw gas chamber 11a and the catalyst layer 15 are separated by a partition plate 14a. The catalyst layer 15 and the reformed gas chamber 11b are separated by a partition plate 14b. The partition plates 14a and 14b are respectively in a disc shape. The partition plates 14a and 14b are formed with a plurality of holes, so that they have air permeability.

[0035] More specifically, a catalyst is filled in a space formed by the inner peripheral surface of the catalyst container 11, the partition plate 14a and the partition plate 14b, thereby forming a catalyst layer 15. The catalyst layer 15 is an aggregate of many granular catalysts, has air permeability and is maintained in a cylindrical shape by the partition plates 14a and 14b. The catalyst is a reforming catalyst for promoting ammonia decomposition reaction, for example, it can be at least one of ruthenium (Ru), nickel (Ni), cobalt (Co) and palladium (Pd), and is not limited to a specific catalyst.

[0036] A heater 16 is disposed in the reformed gas chamber 11 b. The heater 16 is an electric heating device. The heater 16 generates heat by power supplied from a power line (not shown). The heater 16 is, for example, cylindrical (circular plate-shaped) and can be disposed along the inner circumference of the catalyst container 11 .

[0037] Reforming gas pipe

[0038] The reformed gas pipes 17a, 17b, 17c, 17d, 17e, 17f, 17g, 17h, and 17i extend from the reformed gas chamber 11b to the raw gas chamber 11a through the partition plate 14b, the catalyst layer 15, and the partition plate 14a, respectively. Figure 3 As shown, the reformed gas pipe 17a extends coaxially with the axis L1. The reformed gas pipes 17b, 17c, 17d, 17e, 17f, 17g, 17h, and 17i are arranged at equal intervals on a circle centered on the axis L1 and extend parallel to the axis L1.

[0039] The reformed gas branch portion 18 is disposed in the reformed gas chamber 11b and connected to the reformed gas flow path 17. One end of a reformed gas inflow pipe 21 extending coaxially with the axis L1 is connected to the reformed gas branch portion 18 on the side opposite to the reformed gas flow path 17. The other end of the reformed gas inflow pipe 21 is located in the reformed gas chamber 11b. Therefore, the reformed gas chamber 11b and the reformed gas branch portion 18 are connected to each other via the reformed gas inflow pipe 21.

[0040] The reformed gas confluence portion 19 is disposed in the raw gas chamber 11a and connected to the reformed gas flow path 17. One end of a reformed gas outflow pipe 22 extending coaxially with the axis L1 is connected to the reformed gas confluence portion 19 on the side opposite to the reformed gas flow path 17. Therefore, the reformed gas inflow pipe 21 and the reformed gas outflow pipe 22 are connected to each other via the reformed gas flow path 17. The reformed gas outflow pipe 22 extends through the insulating material 13 and the storage container 12. The other end (not shown) of the reformed gas outflow pipe 22 is connected to the adsorption device 92.

[0041] One end of the raw gas inlet pipe 23 is connected to the raw gas chamber 11a from the left side. The raw gas inlet pipe 23 extends through the insulating material 13 and the storage container 12. The other end of the raw gas inlet pipe 23 (not shown) is connected to the ammonia reservoir 91.

[0042] Ammonia reforming

[0043] Ammonia supplied from the ammonia reservoir 91 flows into the raw gas chamber 11 a through the raw gas inflow pipe 23 .

[0044] Next, ammonia flows into the catalyst layer 15 through the plurality of holes formed in the partition plate 14a. The ammonia flowing into the catalyst layer 15 absorbs heat energy while being acted upon by the catalyst and decomposes into hydrogen and nitrogen. These decomposed gases (i.e., reformed gas) flow into the reformed gas chamber 11b through the plurality of holes formed in the partition plate 14b together with undecomposed ammonia.

[0045] The mixed gas (i.e., reformed gas and ammonia) in the reformed gas chamber 11b is heated by the heater 16 to a high temperature. The high-temperature mixed gas flows into the reformed gas flow path 17 via the reformed gas inlet pipe 21 and the reformed gas branch portion 18, and heats the catalyst layer 15 and the ammonia flowing therein. That is, the high-temperature mixed gas and the catalyst exchange heat via the wall of the reformed gas flow path 17. As a result, the catalyst is activated, and the decomposition reaction of ammonia in the catalyst layer 15 is promoted. More specifically, by heat exchange through the tube walls of the plurality of reformed gas pipes 17a, 17b, 17c, 17d, 17e, 17f, 17g, 17h, and 17i, the heat transfer area between the mixed gas and the catalyst layer 15 can be increased, and as a result, a larger portion of the catalyst layer 15 can be maintained at a temperature at which the catalyst is activated.

[0046] First Modification

[0047] Reference Figure 4 A modification of the first embodiment (first modification) will be described. The reformer 1a according to the first modification includes a reformed gas flow path 24, a reformed gas branching portion 27, and a reformed gas converging portion 28 that are different from the reformed gas flow path 17, the reformed gas branching portion 18, and the reformed gas converging portion 19 described above. The reformed gas branching portion 27 and the reformed gas converging portion 28 are formed to form a catalyst container 11 and a storage container 12. Figure 4 The mixed gas flowing into the reformed gas inlet pipe 21 in the reformed gas chamber 11b flows into the reformed gas outlet pipe 22 via the reformed gas branching portion 27, the reformed gas flow path 24 and the reformed gas converging portion 28.

[0048] The reformed gas flow path 24 is formed by 16 reformed gas pipes arranged in a 4×4 matrix (lattice) in a plan view. Figure 4 The reforming gas pipes 24a, 24b, 24c, and 24d (i.e., four gas pipes) are shown in FIG. Figure 4 The visual direction shown ( Figure 4 ), in front of the reforming gas pipe 24a ( Figure 4 There are two gas pipes of the same shape as the reformed gas pipe 24a on the front side of the paper, and on the back side of the reformed gas pipe 24a ( Figure 4 On the inner side of the paper (inside the paper), there is a gas pipe of the same shape as the reforming gas pipe 24a.

[0049] Depend on Figure 4 It can be seen that the reformed gas flow path 24 includes a small diameter portion 25 and a large diameter portion 26. The large diameter portion 26 is a section having a larger outer diameter and inner diameter than the small diameter portion 25. Therefore, when the mixed gas flows from the small diameter portion 25 into the large diameter portion 26, the flow rate of the mixed gas decreases as the inner diameter increases.

[0050] On the other hand, the mixed gas heated by the heater 16 in the reformed gas chamber 11b and becoming high temperature circulates in the reformed gas flow path 24 while heating the catalyst layer 15, so the temperature decreases as it approaches the reformed gas confluence portion 28. In other words, when the temperature of the mixed gas in the reformed gas flow path 24 decreases, the flow rate of the mixed gas decreases, thereby promoting the movement of heat energy to the catalyst layer 15. Therefore, according to the reformer 1a, the temperature gradient between the upper side (the reformed gas branch portion 27 side) and the lower side (the reformed gas confluence portion 28 side) in the catalyst layer 15 can be reduced. As a result, more parts of the catalyst layer 15 can be maintained at a temperature at which the catalyst action is activated.

[0051] Second Embodiment

[0052] One side reference Figure 5 The second embodiment will be described with a focus on the differences from the first embodiment. Figure 5 As shown in FIG. 1 , the reformer 2 of the second embodiment includes a catalyst container 31, an intermediate container 32, an outer container 33, a storage container 34, a heat insulating material 35, a catalyst container outflow pipe 36, partition plates 37a and 37b, a heater 38, a catalyst layer 39, a raw gas inflow pipe 41, and a reformed gas outflow pipe 42. In the following description of the structure of the reformer 2, the up, down, left, and right directions are in the Figure 5 The direction when observing.

[0053] The catalyst container 31, the intermediate container 32, the outer container 33 and the storage container 34 are respectively arranged in Figure 5The dashed line is coaxial with the axis L2. The space formed between the outer wall surface of the outer container 33 and the inner wall surface of the storage container 34 is filled with a heat insulating material 35, which is a well-known heat insulating material.

[0054] A catalyst container inlet 31a is formed on the bottom surface of the catalyst container 31. The catalyst container inlet 31a is a circular opening (circular hole) centered on the axis L2. A catalyst container outflow pipe 36 extending coaxially with the axis L2 is connected to the top surface of the catalyst container 31.

[0055] The catalyst container 31 includes a raw gas chamber 31b, a heater 38, a catalyst layer 39, and a reformed gas chamber 31c. The heater 38 and the catalyst layer 39 are adjacent to the raw gas chamber 31b above the raw gas chamber 31b. The reformed gas chamber 31c is adjacent to the heater 38 and the catalyst layer 39 above the heater 38 and the catalyst layer 39.

[0056] A partition plate 37a is disposed at the upper end of the raw gas chamber 31b. A partition plate 37b is disposed at the lower end of the reformed gas chamber 31c. A heater 38 is disposed on the inner circumference of the catalyst container 31 between the partition plates 37a and 37b. The heater 38 is an electric heating device having a cylindrical shape. A catalyst is filled in a cylindrical space formed by the partition plates 37a, 37b and the inner circumference of the heater 38, thereby forming a catalyst layer 39.

[0057] One end of the raw gas inlet pipe 41 is connected to the upper left portion of the intermediate container 32. The raw gas inlet pipe 41 extends through the outer container 33, the insulating material 35, and the storage container 34. The other end (not shown) of the raw gas inlet pipe 41 is connected to the ammonia reservoir 91.

[0058] One end of a reformed gas outflow pipe 42 is connected to the lower right portion of the outer container 33. The reformed gas outflow pipe 42 extends through the heat insulating material 35 and the storage container 34. The other end (not shown) of the reformed gas outflow pipe 42 is connected to the adsorption device 92.

[0059] Ammonia flowing into the intermediate container 32 from the raw gas inflow pipe 41 flows downward in the outer raw gas flow path 32a formed between the inner wall surface of the intermediate container 32 and the outer wall surface of the catalyst container 31. Next, ammonia flows into the catalyst container 31 (specifically, the raw gas chamber 31b) from the catalyst container inlet 31a. The ammonia flowing into the raw gas chamber 31b flows into the catalyst layer 39 through the partition plate 37a, and absorbs heat energy while being acted on by the catalyst to be decomposed into hydrogen and nitrogen.

[0060] These gases (mixed gas) obtained by decomposition flow into the reformed gas chamber 31c together with undecomposed ammonia through the partition plate 37b. The mixed gas flows into the outer reformed gas flow path 33a formed between the outer wall surface of the intermediate container 32 and the inner wall surface of the outer container 33 through the catalyst container outflow pipe 36, and flows downward. Next, the mixed gas is discharged through the reformed gas outflow pipe 42 and flows to the adsorption device 92.

[0061] Here, the significance of the outer raw gas flow path 32a configured to allow ammonia to flow outside the heater 38 is explained. The heat energy generated by the heater 38 moves from the outer periphery of the catalyst layer 39 (i.e., the area near the outer peripheral surface in contact with the heater 38) to the vicinity of the axis of the catalyst layer 39 (i.e., the area near the axis L2). In addition, the heater 38 not only directly heats the catalyst layer 39 located on the inner side and the ammonia located therein, but also heats the ammonia flowing in the outer raw gas flow path 32a located on the outer side. The ammonia heated by the heater 38 begins to partially decompose before flowing into the catalyst layer 39, and further decomposes under the action of the catalyst after flowing into the catalyst layer 39.

[0062] In addition, the significance of the outer reformed gas flow path 33a configured to allow the mixed gas to flow outside the outer raw gas flow path 32a is explained. The temperature of the ammonia flowing into the outer raw gas flow path 32a from the raw gas inlet pipe 41 is generally lower than the temperature of the mixed gas. Therefore, heat is exchanged between the ammonia flowing in the outer raw gas flow path 32a and the mixed gas flowing in the outer reformed gas flow path 33a. Specifically, the mixed gas is cooled by the ammonia. Therefore, in the adsorption device 92, the process for cooling the inflowing mixed gas can be omitted or labor saving can be achieved. In addition, since the ammonia is heated not only by the heater 38 but also by the mixed gas, the power consumption of the heater 38 can be suppressed.

[0063] Third Embodiment

[0064] One side reference Figure 6 The third embodiment will be described with a focus on the differences from the first embodiment. Figure 6 As shown in FIG. 1 , the reformer 3 of the third embodiment includes a catalyst container 51, a storage container 52, an insulating material 53, partition plates 54a, 54b, a heater 55, a catalyst layer 56, a raw gas inflow path 57, and an inner reformed gas flow path 58. In the following description of the structure of the reformer 3, the up, down, left, and right directions are in the order of Figure 6 The direction when observing.

[0065] The catalyst container 51 and the storage container 52 each have a substantially cylindrical shape, for example, and are arranged so as to Figure 6The dashed line is coaxial with the axis L3. The space formed between the outer wall surface of the catalyst container 51 and the inner wall surface of the storage container 52 is filled with a heat insulating material 53, which is a well-known heat insulating material.

[0066] The catalyst container 51 includes a raw gas chamber 51a, a heater 55, a catalyst layer 56, and a reformed gas chamber 51b therein. The heater 55 and the catalyst layer 56 are adjacent to the raw gas chamber 51a above the raw gas chamber 51a. The reformed gas chamber 51b is adjacent to the heater 55 and the catalyst layer 56 above the heater 55 and the catalyst layer 56. A partition plate 54a is disposed at the upper end of the raw gas chamber 51a. A partition plate 54b is disposed at the lower end of the reformed gas chamber 51b.

[0067] A heater 55 is provided on the inner circumferential surface between the partition plates 54a and 54b of the catalyst container 51. The heater 55 is an electric heating device having a cylindrical shape. A catalyst is filled in the cylindrical space formed by the partition plates 54a, 54b and the inner circumferential surface of the heater 55, thereby forming a catalyst layer 56. The heater 55 generates heat to heat the catalyst layer 56 and the ammonia therein.

[0068] The raw gas inflow passage 57 penetrates the storage container 52, the heat insulating material 53 and the storage container 52, and one end (upper end) on the downstream side is located in the raw gas chamber 51a. The upstream side of the raw gas inflow passage 57 is connected to the ammonia reservoir 91.

[0069] The inner reformed gas flow path 58 includes a catalyst layer penetration portion 58a extending through the catalyst layer 56 and a reformed gas outflow portion 58b that discharges the mixed gas from the reformer 3. One end (upper end) on the upstream side of the inner reformed gas flow path 58 is located in the reformed gas chamber 51b. A portion of the reformed gas outflow portion 58b is arranged in the raw gas inflow path 57. Specifically, the inner reformed gas flow path 58 enters the interior from the outlet of the raw gas inflow path 57, passes through the section (heat exchange section) included in the raw gas inflow path 57 for a short time, and then passes through the wall of the raw gas inflow path 57 and flows out to the outside. The downstream end (not shown) of the raw gas inflow path 57 is connected to the adsorption device 92.

[0070] Ammonia flowing into the raw gas chamber 51a from the raw gas inflow path 57 flows into the catalyst layer 56 via the partition plate 54a, and absorbs heat energy while being acted upon by the catalyst to be decomposed into hydrogen and nitrogen. These decomposed gases (mixed gas) flow into the reformed gas chamber 51b via the partition plate 54b together with undecomposed ammonia. Thereafter, the mixed gas is discharged via the inner reformed gas flow path 58 and flows to the adsorption device 92.

[0071] Here, the significance of the catalyst layer penetration portion 58a of the inner reformed gas flow path 58 is described. The heat energy generated by the heater 55 has an effect on the catalyst layer 56 and the gas flowing therein from the outer peripheral portion of the catalyst layer 56 (i.e., the area near the outer peripheral surface in contact with the heater 55) to the central portion (i.e., Figure 6 The area near the axis L3) is heated.

[0072] On the other hand, the reformed gas and undecomposed ammonia (i.e., mixed gas) flowing out of the catalyst layer 56 become relatively high temperatures. Therefore, the mixed gas flowing through the inner reformed gas flow path 58 heats the catalyst layer 56 and the ammonia flowing therein from the center of the catalyst layer 56 via the wall of the catalyst layer penetration portion 58a. In this way, the catalyst layer 56 can be heated from the center by the high-temperature mixed gas, so that the power consumption of the heater 55 can be suppressed.

[0073] In addition, the significance of a portion of the inner reformed gas flow path 58 being included in the raw gas inlet path 57 is explained. Even after heat exchange with the catalyst, the temperature of the mixed gas flowing through the inner reformed gas flow path 58 downstream of the section penetrating the catalyst layer 56 (i.e., the section below the dividing plate 54a) is relatively high. On the other hand, the ammonia supplied from the ammonia reservoir 91 is not heated and has a relatively low temperature (e.g., 25°C). Therefore, heat exchange is performed between the mixed gas and ammonia via the wall of the inner reformed gas flow path 58 in the heat exchange section. That is, the ammonia is heated before flowing into the raw gas chamber 51a.

[0074] Since the temperature of ammonia increases due to heat exchange between ammonia and the mixed gas, it contributes to the increase in the temperature of the catalyst, thereby suppressing the power consumption of the heater 55. On the other hand, since the temperature of the mixed gas decreases due to heat exchange, the burden of cooling the mixed gas in the adsorption device 92 is reduced.

[0075] As described above, according to the reformers 1 , 1 a , 2 , 3 of the respective embodiments, it is possible to avoid excessive power consumption of the heaters 16 , 38 , 55 .

[0076] Other Implementations

[0077] In the above-mentioned embodiment, the raw gas is ammonia and the reformed gas contains hydrogen and nitrogen. As another embodiment, the main components of the raw gas may be methane gas (CH4) and water vapor (H2O) and the reformed gas may contain carbon dioxide (CO2) and hydrogen. That is, the reformers 1, 1a, 2, 3 may also be configured to decompose methane gas by a steam reforming reaction using a catalyst of an appropriate type and form. In addition, the steam reforming reaction of methane gas is an endothermic reaction.

[0078] The heaters 16, 38, and 55 are electrical heating devices. As another embodiment, these heating devices may be heating devices other than electrical heating devices. For example, the heating device may be configured to generate heat by introducing high-temperature water vapor exhausted from the fuel cell 93.

[0079] The catalyst layers 15, 39, and 56 are aggregates of granular catalysts. As another embodiment, the catalyst layer may be formed by supporting an active component (catalyst substance) such as ruthenium and nickel on a porous carrier (base material).

[0080] Figure 2 and Figure 3 The reformer 1 includes 9 reforming gas pipes extending in a straight line (i.e., a reforming gas pipe 17a extending coaxially with the axis L1 and reforming gas pipes 17b, 17c, 17d, 17e, 17f, 17g, 17h, 17i arranged on a circle centered on the axis L1). As other embodiments, the central reforming gas pipe 17a may be omitted. Alternatively, as other embodiments, the number of reforming gas pipes may be different from 9. As yet another embodiment, the reforming gas flow path 17 may not extend in a straight line. For example, the reforming gas pipes 17b, 17c, 17d, 17e, 17f, 17g, 17h, 17i may respectively extend from the reforming gas branch portion 18 while twisting toward the reforming gas confluence portion 19.

[0081] Figure 4 The reformed gas flow path 24 of the reformer 1a includes a small diameter portion 25 and a large diameter portion 26. That is, the outer diameter and the inner diameter of the reformed gas flow path 24 change in two stages in a manner that the inner diameter increases downstream of the mixed gas in the catalyst layer. As another embodiment, the outer diameter and the inner diameter of the reformed gas flow path 24 may be changed in three stages in a manner that the inner diameter increases downstream of the mixed gas. Alternatively, as another embodiment, the outer diameter and the inner diameter of the reformed gas flow path 24 may be continuously increased as they approach the downstream of the mixed gas.

[0082] Figure 2 The heater 16 of the reformer 1 is disposed on the inner peripheral surface of the catalyst container 11. As another embodiment, the heater 16 may be disposed on the outer peripheral surface of the catalyst container 11 to heat the mixed gas in the reformed gas chamber 11b.

[0083] Figure 6 The inner peripheral surface of the heater 55 of the reformer 3 is in contact with the outer peripheral surface of the catalyst layer 56. As another embodiment, a space may be formed between the inner peripheral surface of the heater 55 and the outer peripheral surface of the catalyst layer 56.

[0084] exist Figure 6In the reformer 3, in order to promote heat exchange between ammonia and the mixed gas, the raw gas inflow path 57 and the inner reformed gas flow path 58 have a heat exchange section. That is, the raw gas inflow path 57 and the inner reformed gas flow path 58 include a section that functions as a double-tube heat exchanger. As another embodiment, the raw gas inflow path 57 and the inner reformed gas flow path 58 may also include a section where the outer peripheral surfaces of each other are connected and twisted in a spiral shape as a heat exchange section to promote heat exchange between ammonia and the mixed gas.

[0085] Various embodiments have been described above with reference to the above-mentioned system, but it is obvious to those skilled in the art that various substitutions, improvements, and changes can be made without departing from the purpose of the present technology. Therefore, the method of the present technology can include all substitutions, improvements, and changes that do not depart from the main purpose and purpose of the technical solution.

Claims

1. A reformer, characterized in that: have: A catalyst container including a section where a catalyst layer is formed, wherein a raw gas flowing in from one end surface of the catalyst layer generates a reformed gas through a reforming reaction accompanied by endothermic reaction when passing through the catalyst layer, and the reformed gas flows out from the other end surface of the catalyst layer; A plurality of reformed gas pipes, penetrating the catalyst layer and allowing the reformed gas to flow; and The heating device heats the reformed gas in a section from when the reformed gas flows out of the catalyst layer to when the reformed gas flows into the plurality of reformed gas pipes.

2. The reformer according to claim 1, characterized in that The inner diameters of the plurality of reformed gas pipes increase toward the downstream of the reformed gas in the catalyst layer.

3. A reformer, characterized in that: have: A catalyst container including a section where a catalyst layer is formed, wherein a raw gas flowing in from one end surface of the catalyst layer generates a reformed gas through a reforming reaction accompanied by endothermic reaction when passing through the catalyst layer, and the reformed gas flows out from the other end surface of the catalyst layer; A heating device, for heating at least the catalyst layer; and The heat exchange unit is used to exchange heat between the reformed gas and the raw gas before flowing into the catalyst layer.

4. The reformer according to claim 3, characterized in that: have: an outer raw material gas flow path configured so that the raw material gas flows outside the catalyst container; and The outer reformed gas flow path is configured so that the reformed gas flows outside the outer raw gas flow path. The heating device is disposed outside the catalyst layer and inside the outer raw gas flow path, and heats the raw gas flowing through the catalyst layer and the outer raw gas flow path. The heat exchange section is composed of the outer reformed gas flow path and the outer raw gas flow path.

5. The reformer according to claim 3, characterized in that: have: a raw material gas inflow path configured to introduce the raw material gas into the catalyst layer; and an inner reformed gas flow path, which is configured to penetrate the catalyst layer and allow the reformed gas to flow through; The heating device is disposed outside the catalyst layer. The heat exchange portion is constituted by a section of the inner reformed gas flow path that is located downstream of the catalyst layer and the raw gas inflow path.

6. The reformer according to any one of claims 1 to 5, characterized in that: The raw material gas is ammonia gas, and the reformed gas is a gas containing hydrogen gas and nitrogen gas generated by decomposition of the ammonia gas.

Images