JP2006232611A

JP2006232611A - Steam reformer for hydrocarbon fuel

Info

Publication number: JP2006232611A
Application number: JP2005049328A
Authority: JP
Inventors: Jun Komiya; 純小宮
Original assignee: Tokyo Gas Co Ltd
Current assignee: Tokyo Gas Co Ltd
Priority date: 2005-02-24
Filing date: 2005-02-24
Publication date: 2006-09-07
Anticipated expiration: 2025-02-24
Also published as: JP4550617B2

Abstract

<P>PROBLEM TO BE SOLVED: To obtain a compact steam reformer with high efficiency particularly by placing a CO removal catalyst layer in a specified layout in a steam reformer, and to obtain a steam reformer with reduced production cost by decreasing the number of components or labors such as installing a heat insulating material or piping for the production of the reformer. <P>SOLUTION: The steam reformer for a hydrocarbon fuel comprises a reforming catalyst portion, a CO conversion catalyst portion and a CO removal catalyst portion, segmented in respective separated layers and integrated in a cylindrical container where a gas passes through the layers in the axial direction. The reformer is characterized in that the CO removal catalyst portion is segmented into a first CO removal catalyst portion and a second CO removal catalyst portion by a cylindrical barrier wall parallel to the axial direction of the cylindrical container, and that the reformer is provided with a gas passage returning from the exit of the first CO removal catalyst portion to the entrance of the second CO removal catalyst portion. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

本発明は、炭化水素系燃料の水蒸気改質器に関し、より詳しくは改質部、ＣＯ変成部、ＣＯ除去部を一体化した水蒸気改質器の構造に関する。特に、燃料電池に水素を供給する、都市ガスやＬＰＧなどの炭化水素系燃料からの水素製造装置として、円筒状容器内に改質触媒、ＣＯ変成触媒、ＣＯ除去触媒などの複数の触媒をそれぞれ別層に区画して配置して一体に構成された水蒸気改質器に関する。 The present invention relates to a steam reformer for hydrocarbon fuel, and more particularly to a structure of a steam reformer in which a reforming section, a CO conversion section, and a CO removal section are integrated. In particular, as a hydrogen production device that supplies hydrogen to a fuel cell from a hydrocarbon-based fuel such as city gas or LPG, a plurality of catalysts such as a reforming catalyst, a CO shift catalyst, and a CO removal catalyst are provided in a cylindrical container. The present invention relates to a steam reformer configured by being divided into separate layers and configured integrally.

例えば固体高分子形燃料電池（以下適宜“ＰＥＦＣ”と略称する）等の燃料電池に炭化水素系燃料を改質して水素を供給するには、水蒸気改質触媒、ＣＯ変成触媒、ＣＯ除去触媒などの複数の触媒が使用される。それらの触媒をそれぞれ充填した反応器を別体として設置した場合、各反応器間を接続する配管や断熱材などが必要となり、機器構成が煩雑になる。そのため、それらの簡素化や小型化を目指し、それぞれの反応器を一体化した燃料処理装置すなわち一体型水蒸気改質器が開発されている。図１はその一例を示す図で、縦断面図として示している（ＷＯ０２／０９８７９０Ａ、特願２００４−１５１５）。 For example, a steam reforming catalyst, a CO conversion catalyst, and a CO removal catalyst are used to reform a hydrocarbon-based fuel and supply hydrogen to a fuel cell such as a polymer electrolyte fuel cell (hereinafter abbreviated as “PEFC” where appropriate). A plurality of catalysts are used. When the reactors filled with the respective catalysts are installed as separate bodies, piping and heat insulating materials for connecting the reactors are required, and the equipment configuration becomes complicated. Therefore, with the aim of simplifying and miniaturizing them, a fuel processing apparatus in which the respective reactors are integrated, that is, an integrated steam reformer has been developed. FIG. 1 is a view showing an example thereof, and is shown as a longitudinal sectional view (WO 02 / 098790A, Japanese Patent Application No. 2004-1515).

ＷＯ０２/０９８７９０ＡWO 02 / 098790A 特願２００４−１５１５Japanese Patent Application No. 2004-1515

図１のとおり、中心軸を同一にして設けられた径の異なる複数の円筒体を間隔を置いて多重に配置して構成される。図１中、一点鎖線はその中心軸を示し、矢印はその方向、すなわちその軸方向を示している。径（＝直径、以下同じ）を順次大きくした、第１円筒体１、第２円筒体２及び第３円筒体３が中心軸を同一にして間隔を置いて配置されている。第３円筒体３の上部には第３円筒体３より径を大きくした第４円筒体４が配置されている。第１円筒体１の内側には中心軸を同じくして、第１円筒体１より径の小さい円筒状の伝熱隔壁すなわち輻射筒５が配置され、輻射筒５内にはバーナー６が配置されている。すなわち、バーナー６は、中心軸部に配置され、輻射筒５の内側に上蓋兼バーナー取付台７を介して取り付けられている。 As shown in FIG. 1, a plurality of cylindrical bodies having the same central axis and having different diameters are arranged in multiple positions at intervals. In FIG. 1, the alternate long and short dash line indicates the central axis, and the arrow indicates the direction, that is, the axial direction. A first cylindrical body 1, a second cylindrical body 2, and a third cylindrical body 3 having diameters (= diameters, the same applies hereinafter) that are sequentially increased are arranged with the same central axis and spaced from each other. A fourth cylinder 4 having a diameter larger than that of the third cylinder 3 is disposed on the third cylinder 3. Inside the first cylindrical body 1, a cylindrical heat transfer partition wall, that is, a radiation cylinder 5 having the same central axis as the diameter of the first cylindrical body 1 is arranged, and a burner 6 is arranged in the radiation cylinder 5. ing. That is, the burner 6 is disposed at the central shaft portion and is attached to the inside of the radiation tube 5 via the upper lid / burner mounting base 7.

輻射筒５は、その下端と第１円筒体１の底板８との間に間隔を設けて配置してあり、この間隙と、これに連なる輻射筒５と第１円筒体１との間の空隙とがバーナー６からの燃焼排ガスの排気通路９を形成している。底板８は第１円筒体１の径に対応した径で円盤状に構成されている。排気通路９は、その上部で排気通路９の上蓋（上蓋兼バーナー取付台７の下面）と隔壁１０（後述予熱層１４の上蓋）との間の間隙を経て燃焼排ガスの排出口１１に連なり、燃焼排ガスはここから排出される。 The radiation cylinder 5 is disposed with a gap between the lower end thereof and the bottom plate 8 of the first cylindrical body 1, and this gap and a gap between the radiation cylinder 5 and the first cylindrical body 1 connected to the clearance are provided. Form an exhaust passage 9 for combustion exhaust gas from the burner 6. The bottom plate 8 is formed in a disc shape with a diameter corresponding to the diameter of the first cylindrical body 1. The exhaust passage 9 is connected to the exhaust port 11 of the combustion exhaust gas through a gap between the upper cover of the exhaust passage 9 (the upper surface of the upper cover and burner mounting base 7) and the partition wall 10 (the upper cover of the preheating layer 14 described later) at the upper part. Combustion exhaust gas is discharged from here.

１２は炭化水素系原料ガスの供給管であり、第１円筒体１と第２円筒体２との間の空間内には、その上部に予熱層１４、これに続く下部に改質触媒層１６が設けられている。なお、第２円筒体２は、改質触媒層１６を囲む部分と予熱層１４を囲む部分とが別個に構成され、改質触媒層１６を囲む上端部と予熱層１４を囲む下端部との間の接合部で接合されているが、接合部を設けることなく一体に構成してもよい。また、改質触媒層１６の触媒は、その下部で多孔板等で支持されているが、その記載は省略している。予熱層１４の内部に一本の丸棒１５が螺旋状に配置され、これにより予熱層１４の内部に一つの連続した螺旋状のガス通路が形成されている。 Reference numeral 12 denotes a hydrocarbon-based source gas supply pipe. In the space between the first cylindrical body 1 and the second cylindrical body 2, a preheating layer 14 is formed in the upper part, and a reforming catalyst layer 16 is formed in the lower part. Is provided. The second cylindrical body 2 is configured such that a portion surrounding the reforming catalyst layer 16 and a portion surrounding the preheating layer 14 are configured separately, and an upper end portion surrounding the reforming catalyst layer 16 and a lower end portion surrounding the preheating layer 14 are formed. Although it joins by the junction part in between, you may comprise integrally, without providing a junction part. Moreover, although the catalyst of the reforming catalyst layer 16 is supported by a porous plate or the like at the lower part, the description thereof is omitted. A single round bar 15 is spirally arranged inside the preheating layer 14, thereby forming one continuous spiral gas passage inside the preheating layer 14.

原料ガスは、供給管１２から供給され、水（水蒸気）が混合部１３で混合された後、予熱層１４を経て、改質触媒層１６に導入される。改質触媒層１６では、炭化水素系原料ガスが下降しながら水蒸気により改質される。炭化水素系原料ガスが例えばメタンガスの場合、反応式：ＣＨ₄＋Ｈ₂Ｏ→３Ｈ₂＋ＣＯの反応で改質される。改質触媒層１６における改質反応は吸熱反応であり、バーナー６で発生する燃焼熱を吸収して反応が進行する。具体的には、バーナー６による燃焼排ガスが輻射筒５と第１円筒体１との間の排気通路９を流通して通過するときに、燃焼排ガスの熱が改質触媒層１６に吸収され、改質反応が行われる。 The raw material gas is supplied from the supply pipe 12, and water (water vapor) is mixed in the mixing unit 13, and then introduced into the reforming catalyst layer 16 through the preheating layer 14. In the reforming catalyst layer 16, the hydrocarbon-based raw material gas is reformed by steam while descending. When the hydrocarbon-based raw material gas is, for example, methane gas, it is reformed by a reaction of reaction formula: CH ₄ + H ₂ O → 3H ₂ + CO. The reforming reaction in the reforming catalyst layer 16 is an endothermic reaction, and the reaction proceeds by absorbing the combustion heat generated in the burner 6. Specifically, when the combustion exhaust gas from the burner 6 flows through the exhaust passage 9 between the radiation cylinder 5 and the first cylindrical body 1, the heat of the combustion exhaust gas is absorbed by the reforming catalyst layer 16, A reforming reaction is performed.

第２円筒体２の下端は第３円筒体３の底板１７との間に間隔を置いて配置してあり、第２円筒体２と第３円筒体３との間は、改質ガスの流路１８を構成している。底板１７は第３円筒体３の径に対応した径で円盤状に構成されている。改質ガスは、第２円筒体２の下端と第３円筒体３の底板１７との間で折り返して第２円筒体２と第３円筒体３との間で形成された流路１８を流通する。第３円筒体３の上部には第３円筒体３より径を大きくした第４円筒体４が配置され、第２円筒体２と第４円筒体４との間にＣＯ変成触媒層２１が設けられている。 The lower end of the second cylindrical body 2 is spaced from the bottom plate 17 of the third cylindrical body 3, and the flow of the reformed gas is between the second cylindrical body 2 and the third cylindrical body 3. A path 18 is formed. The bottom plate 17 is configured in a disc shape with a diameter corresponding to the diameter of the third cylindrical body 3. The reformed gas is folded between the lower end of the second cylindrical body 2 and the bottom plate 17 of the third cylindrical body 3 and flows through the flow path 18 formed between the second cylindrical body 2 and the third cylindrical body 3. To do. A fourth cylindrical body 4 having a diameter larger than that of the third cylindrical body 3 is disposed on the third cylindrical body 3, and a CO shift catalyst layer 21 is provided between the second cylindrical body 2 and the fourth cylindrical body 4. It has been.

第３円筒体３の上端部と第４円筒体４の下端部には板体１９（第３円筒体３の直径に相当する部分は第３円筒体３で占められるので、ドーナツ状の板体）が配置され、板体１９の上に、間隔を置いてガス流通用の複数の孔を有する支持板２０（第２円筒体２の直径に相当する部分は第２円筒体２で占められるので、ドーナツ状の支持板）が配置されている。ＣＯ変成触媒層２１は、支持板２０とガス流通用の複数の孔を有する支持板２２（第２円筒体２の直径に相当する部分は第２円筒体２で占められるのでドーナツ状の支持板、ＣＯ変成触媒層２１の上蓋）との間に設けられている。支持板２０、２２は金属製等の網目体で構成してもよく、この場合には網目体の網目がガス流通孔となる。流路１８を流通した改質ガスは、支持板２０の孔を経てＣＯ変成触媒層２１に供給される。 A plate 19 (a portion corresponding to the diameter of the third cylinder 3 is occupied by the third cylinder 3 at the upper end of the third cylinder 3 and the lower end of the fourth cylinder 4. ) And a support plate 20 having a plurality of holes for gas circulation at intervals on the plate body 19 (the portion corresponding to the diameter of the second cylinder 2 is occupied by the second cylinder 2). , A donut-shaped support plate) is disposed. The CO shift catalyst layer 21 includes a support plate 20 and a support plate 22 having a plurality of holes for gas circulation (the portion corresponding to the diameter of the second cylindrical body 2 is occupied by the second cylindrical body 2, so a donut-shaped support plate And the upper cover of the CO shift catalyst layer 21). The support plates 20 and 22 may be formed of a mesh body made of metal or the like. In this case, the mesh body of the mesh body serves as a gas flow hole. The reformed gas that has flowed through the flow path 18 is supplied to the CO shift catalyst layer 21 through the holes of the support plate 20.

上記のとおり、ＣＯ変成触媒層２１は、第２円筒体２と第４円筒体４との間に設けられているが、第４円筒体４の外周には間隔を置いて円筒体２４が配置され、その間に断熱材２３が配置されている。円筒体２４の外周にはプロセス水、すなわち原料ガス改質用の水の供給管２５から連なる伝熱管２６が直接螺旋状に巻き付けてある。伝熱管２６はＣＯ変成触媒層２１を間接的に冷却する冷却機構として作用する。断熱材２３は、伝熱管２６の冷却作用により、ＣＯ変成触媒層１２の温度を低下させ過ぎず、適度な温度に均一に保持できる厚さに巻き付けてある。断熱材２３としては好ましくはセラミックファイバーナーどの加工性のよいものを用いる。ここで、伝熱管２６は、水供給管２５から供給される水のボイラーとしての機能を備え、また水供給管２５から続く連続した一つの通路となっているので、複数の通路では生じる部分的な滞留等が生じない。 As described above, the CO conversion catalyst layer 21 is provided between the second cylindrical body 2 and the fourth cylindrical body 4, and the cylindrical body 24 is arranged on the outer periphery of the fourth cylindrical body 4 with a space therebetween. The heat insulating material 23 is disposed between them. A heat transfer pipe 26 connected from a supply pipe 25 of process water, that is, raw material gas reforming water, is directly wound around the outer periphery of the cylindrical body 24 in a spiral shape. The heat transfer tube 26 acts as a cooling mechanism for indirectly cooling the CO shift catalyst layer 21. The heat insulating material 23 is wound to a thickness that can be uniformly maintained at an appropriate temperature without excessively reducing the temperature of the CO shift catalyst layer 12 by the cooling action of the heat transfer tube 26. As the heat insulating material 23, a ceramic fiberner having good workability is preferably used. Here, the heat transfer pipe 26 has a function as a boiler for the water supplied from the water supply pipe 25 and is a continuous single passage that continues from the water supply pipe 25, so that partial heat generation occurs in a plurality of passages. Stagnation does not occur.

ＣＯ変成触媒層２１では、反応式：ＣＯ＋Ｈ₂Ｏ→ＣＯ₂＋Ｈ₂で示されるＣＯ変成反応（water gas shift reaction）、すなわちシフト反応が行われ、改質ガス中のＣＯが二酸化炭素に変成され、併せて水素が生成する。 In the CO shift catalyst layer 21, a CO shift reaction (water gas shift reaction) represented by a reaction formula: CO + H ₂ O → CO ₂ + H ₂ , that is, a shift reaction is performed, and CO in the reformed gas is converted into carbon dioxide. Together, hydrogen is produced.

ＣＯ変成触媒としては、従来の触媒（すなわちＣｕ／Ｚｎ系低温ＣＯ変成触媒等）でもよいが、少なくとも３５０℃以上で連続して使用できる触媒（すなわち白金系やＦｅ／Ｃｒ系の高温ＣＯ変成触媒等）を用いることにより、改質ガスの流路１８やＣＯ変成触媒層２１の長さ（すなわち支持板２０と支持板２２と間の長さ）を短縮できる。これにより触媒反応装置（改質器）全体を小型化、軽量化できる。白金系触媒すなわち白金を主成分とした触媒はアルミナ等の担体に白金を担持して構成される。白金を主成分とした触媒は、酸化などによる劣化にも強く、３５０℃以上の高温域、特に４００℃以上の高温域でも連続して使用することが可能であり、より速い速度で反応を進行させることができる。 The CO conversion catalyst may be a conventional catalyst (that is, a Cu / Zn-based low temperature CO conversion catalyst, etc.), but a catalyst that can be used continuously at least at 350 ° C. or higher (that is, a platinum-based or Fe / Cr-based high-temperature CO conversion catalyst). Etc.) can be used to shorten the length of the reformed gas flow path 18 and the CO shift catalyst layer 21 (that is, the length between the support plate 20 and the support plate 22). As a result, the entire catalytic reaction device (reformer) can be reduced in size and weight. A platinum-based catalyst, that is, a catalyst containing platinum as a main component is configured by supporting platinum on a carrier such as alumina. Platinum-based catalysts are resistant to deterioration due to oxidation, etc., and can be used continuously even in a high temperature range of 350 ° C or higher, particularly in a high temperature range of 400 ° C or higher, and the reaction proceeds at a faster rate. Can be made.

支持板２２の上方には所定の間隔を置いて一つの連通孔２８を有する仕切板２７が設けてあり、両板間の空間に空気の供給管２９を通してＣＯ除去用空気が供給される。仕切板２７の上方には円環状の通路３０が設けてある。連通孔２８を所定の孔径で且つ一つとすることにより、改質ガスとＣＯ除去用空気が連通孔２８を通過する際に所定の通過速度が得られ、通過時の乱流により改質ガスとＣＯ除去用空気を良好に混合することができる。 A partition plate 27 having one communication hole 28 is provided above the support plate 22 at a predetermined interval, and CO removal air is supplied to the space between both plates through an air supply pipe 29. An annular passage 30 is provided above the partition plate 27. By using one communication hole 28 with a predetermined hole diameter, a predetermined passing speed is obtained when the reformed gas and the CO removal air pass through the communication hole 28, and the reformed gas and CO removal air can be mixed well.

ＣＯ除去触媒層３５は、（ａ）第２円筒体２と（ｂ）これより径を大きくした円筒体３６と（ｃ）第２円筒体２と円筒体３６との間の下部及び上部にそれぞれ間隔を置いて配置された、複数個の孔３４を有する支持板３３（第２円筒体２の直径に相当する部分は第２円筒体２で占められるので、ドーナツ状の板体）と（ｄ）ガス流通用の複数個の孔３８を有する支持板３７（第２円筒体２の直径に相当する部分は第２円筒体２で占められるので、ドーナツ状の支持板）との間の空間に設けられている。 The CO removal catalyst layer 35 includes (a) a second cylindrical body 2, (b) a cylindrical body 36 having a larger diameter, and (c) a lower portion and an upper portion between the second cylindrical body 2 and the cylindrical body 36, respectively. A support plate 33 having a plurality of holes 34 arranged at intervals (a portion corresponding to the diameter of the second cylindrical body 2 is occupied by the second cylindrical body 2), and (d ) A support plate 37 having a plurality of holes 38 for gas distribution (the portion corresponding to the diameter of the second cylindrical body 2 is occupied by the second cylindrical body 2), so that it is in a space between the support plate 37 and the donut-shaped support plate. Is provided.

円筒体３６の下部にはその円周方向に均等ないしほぼ均等に複数個の孔３２が設けられている。円環状の通路３０は、円筒体２４と仕切板２７と仕切板３１と円筒体３６で形成された通路であり、それら複数個の孔３２と支持板３３の複数個の孔３４を介してＣＯ除去触媒層３５に連通しており、ＣＯ除去用空気が混合された改質ガスがそれらを介してＣＯ除去触媒層３５に導入される。ＣＯ除去触媒層３５は、その上蓋である複数個の孔３８を有する仕切板３７と隔壁１０との間の間隙を介して改質ガスの取出管３９に連通している。また、ＣＯ除去触媒層３５は円筒体３６で囲まれているが、円筒体３６の外周には円筒体２４の外周の伝熱管２６から連なる伝熱管２６が直接螺旋状に巻き付けてある。 A plurality of holes 32 are provided in the lower part of the cylindrical body 36 equally or substantially uniformly in the circumferential direction. The annular passage 30 is a passage formed by the cylindrical body 24, the partition plate 27, the partition plate 31, and the cylindrical body 36, and the CO is passed through the plurality of holes 32 and the plurality of holes 34 of the support plate 33. The reformed gas that is in communication with the removal catalyst layer 35 and mixed with the CO removal air is introduced into the CO removal catalyst layer 35 through them. The CO removal catalyst layer 35 communicates with a reformed gas take-out pipe 39 through a gap between a partition plate 37 having a plurality of holes 38 serving as an upper lid and the partition wall 10. Further, the CO removal catalyst layer 35 is surrounded by a cylindrical body 36, and a heat transfer tube 26 connected to the heat transfer tube 26 on the outer periphery of the cylindrical body 24 is directly spirally wound around the outer periphery of the cylindrical body 36.

ＣＯ除去触媒層３５には、ＣＯ除去触媒（＝ＰＲＯＸ触媒）が充填してあり、ＰＲＯＸ触媒によりＣＯ除去反応が行われ、改質ガス中のＣＯ含有量をｐｐｍ単位にまで低減する。ＣＯ除去触媒としては、改質ガス中のＣＯを選択的に酸化し得る触媒であれば特に限定はなく、例えばＲｕ系などの金属触媒が用いられる。金属触媒は、例えばアルミナ等の担体にＲｕなどの金属触媒を担持させて構成される。ＣＯ除去触媒層３５においては、反応式：２ＣＯ＋Ｏ₂→２ＣＯ₂で示されるＣＯ除去反応が進行する。 The CO removal catalyst layer 35 is filled with a CO removal catalyst (= PROX catalyst), and a CO removal reaction is performed by the PROX catalyst to reduce the CO content in the reformed gas to the ppm unit. The CO removal catalyst is not particularly limited as long as it can selectively oxidize CO in the reformed gas. For example, a Ru-based metal catalyst is used. The metal catalyst is configured by supporting a metal catalyst such as Ru on a carrier such as alumina. In the CO removal catalyst layer 35, the CO removal reaction represented by the reaction formula: 2CO + O ₂ → 2CO ₂ proceeds.

ＣＯ除去触媒層３５においてＣＯを除去した改質ガスは、その上蓋である仕切板３７に設けられた複数個の孔３８から排出され、仕切板３７と隔壁１０との間の間隙を経て改質ガスの取出管３９から取り出される。第３円筒体３、円筒体２４及び円筒体３６を含む外周部には断熱材４０を配置し、外部への熱の放散を防止している。断熱材４０としては、例えばマイクロサーム、ケイ酸カルシウム、アルミナファイバーなど、断熱効果の高い断熱材が使用される。 The reformed gas from which CO has been removed in the CO removal catalyst layer 35 is discharged from a plurality of holes 38 provided in the partition plate 37 which is the upper lid, and reformed through the gap between the partition plate 37 and the partition wall 10. The gas is extracted from the gas extraction pipe 39. A heat insulating material 40 is disposed on the outer peripheral portion including the third cylindrical body 3, the cylindrical body 24, and the cylindrical body 36 to prevent heat from being dissipated to the outside. As the heat insulating material 40, for example, a heat insulating material having a high heat insulating effect such as microtherm, calcium silicate, alumina fiber or the like is used.

図２は、図１中ＣＯ除去触媒層３５の部分を中心に拡大して示した図である。図２のとおり、円筒体３６の下部にその円周方向に均等ないしほぼ均等に設けられた複数個の孔３２から導入されたＣＯ除去用空気が混合された改質ガスは、ＣＯ除去触媒層３５中を上昇しながら、ＣＯが酸化除去され、その上部から導出される。すなわち、ＣＯ除去用空気が混合された改質ガスは、厚みをもつドーナツ状のＣＯ除去触媒層３５中を下方から上方へ向かって、すなわちＣＯ除去触媒層３５を区画する第２円筒体２及び円筒体３６の軸方向に流れる。改質ガスの取出管３９は、例えばＰＥＦＣへの燃料ガス供給管に接続される。この場合、所定の濃度の水素を含有する改質ガスがＰＥＦＣの燃料極側に供給され、これを燃料として発電される。なお、ＰＥＦＣの燃料極からのオフガス（アノードオフガス）を、バーナー６での燃焼用燃料ガスとして使用してもよい。 FIG. 2 is an enlarged view centering on the portion of the CO removal catalyst layer 35 in FIG. As shown in FIG. 2, the reformed gas mixed with the CO removal air introduced from the plurality of holes 32 provided at the lower portion of the cylindrical body 36 in the circumferential direction is provided with the CO removal catalyst layer. While rising in 35, CO is oxidized and removed from the top. That is, the reformed gas mixed with the CO removal air passes through the doughnut-shaped CO removal catalyst layer 35 having a thickness from the lower side to the upper side, that is, the second cylindrical body 2 defining the CO removal catalyst layer 35 and It flows in the axial direction of the cylindrical body 36. The reformed gas take-out pipe 39 is connected to, for example, a fuel gas supply pipe to the PEFC. In this case, a reformed gas containing a predetermined concentration of hydrogen is supplied to the fuel electrode side of the PEFC, and electricity is generated using this as a fuel. Note that off-gas (anode off-gas) from the fuel electrode of PEFC may be used as fuel gas for combustion in the burner 6.

ところで、以上のように構成された水蒸気改質器において用いられる各触媒は、それぞれ、ガス空間速度ＳＶ、ガス線速度ＬＶ、温度条件などの異なる特性、環境で使用されるため、装置設計上の制約がある。水蒸気改質器のうち、例えばＰＥＦＣ用の水蒸気改質器に用いられる各触媒の特性は以下のとおりである。
（１）改質触媒：反応速度が大きく、伝熱律速の反応形態であるため（伝熱面積が大きいため）、ガス流れ軸方向に長くなる。また、温度が高いため、断熱材が厚くなる。
（２）ＣＯ変成触媒：反応速度が遅いため、触媒量が多くなる。そのため、ガス空間速度ＳＶが小さく、ガスの流れ軸方向に大きい反応器となる。
（３）ＣＯ除去触媒：ガス線速度ＬＶが大きいため、ガス流れ軸方向に長くなる。また、温度が低いため、断熱材は薄くてもよい。 By the way, each catalyst used in the steam reformer configured as described above is used in different characteristics and environments such as gas space velocity SV, gas linear velocity LV, temperature conditions, etc. There are limitations. Among the steam reformers, for example, the characteristics of each catalyst used in the steam reformer for PEFC are as follows.
(1) Reforming catalyst: Since the reaction rate is high and the heat transfer rate-controlled reaction mode (because the heat transfer area is large), the reforming catalyst becomes longer in the gas flow axis direction. Moreover, since temperature is high, a heat insulating material becomes thick.
(2) CO conversion catalyst: Since the reaction rate is slow, the amount of catalyst increases. Therefore, the gas space velocity SV is small and the reactor is large in the gas flow axis direction.
(3) CO removal catalyst: Since the gas linear velocity LV is large, it becomes longer in the gas flow axis direction. Further, since the temperature is low, the heat insulating material may be thin.

前述のような従来の水蒸気改質器においては、各触媒はともに、ガス流れ軸方向に沿って順次区画して設置されるため、すなわち円筒状容器の軸方向と同じ方向にガスが流通するように順次区画して設置されるため、前述図１〜２に示すような形状となる。このうち、特にＣＯ除去触媒が充填された区画は、ＣＯ変成触媒が充填された区画に対して、径方向に小さくなるため、これらを一体に配置した触媒反応装置の外形が段階状の複雑な構造となる。そのため、部品点数が多く、断熱材や配管施工などに手間がかかるため、製作コストが高くなり、また、ガスの流れ軸方向に小型化できないなどの問題があった。 In the conventional steam reformer as described above, each of the catalysts is sequentially partitioned along the gas flow axis direction, that is, the gas flows in the same direction as the axial direction of the cylindrical container. Are sequentially partitioned and thus have the shape shown in FIGS. Among these, especially the section filled with the CO removal catalyst is smaller in the radial direction than the section filled with the CO shift catalyst, and therefore, the outer shape of the catalyst reaction apparatus in which these are integrally arranged is a complicated stepwise shape. It becomes a structure. As a result, the number of parts is large, and it takes time to construct the heat insulating material and piping, resulting in high manufacturing costs and a problem that the gas flow cannot be reduced in the axial direction.

それらの問題のうち、特に小型化できない点は、その分上蓋、下蓋を含めた外周面積が大きく、熱エネルギーの損失を招くたげでなく、家庭用コージェネレーションシステムなどで使用する場合、設置スペースの制約に応え得ないことになってしまう。 Among these problems, the size of the area that cannot be reduced in particular is large, so the outer area including the upper and lower lids is large, which does not lead to loss of heat energy. It will not be possible to meet the restrictions.

また、改質ガス中のＣＯを確実に低減するために、特性の異なるＣＯ除去触媒を積層して配置する方法も考えられている（特開平１１−３１０４０２号公報）。この配置方法を前述図１〜２のような水蒸気改質器に適用すると図３〜４のようになる。図３において、ＣＯ除去触媒部が４１と４２との二段になり、図１〜２に比べて、その分（二段にした分）、円筒状容器の軸方向に長くなってしまう。図４は、二段目のＣＯ除去触媒部４２にもＣＯ除去用空気を導入するようにしたものであるが、円筒状容器の軸方向に長くなってしまう点では図３の場合と同様である。 In order to reliably reduce CO in the reformed gas, a method of stacking and arranging CO removal catalysts having different characteristics has been considered (Japanese Patent Laid-Open No. 11-310402). When this arrangement method is applied to the steam reformer as shown in FIGS. In FIG. 3, the CO removal catalyst part is composed of two stages 41 and 42, and is longer in the axial direction of the cylindrical container than that in FIGS. FIG. 4 shows the case where CO removal air is introduced also into the second stage CO removal catalyst section 42, but is the same as the case of FIG. 3 in that it becomes longer in the axial direction of the cylindrical container. is there.

特開平１１−３１０４０２号公報JP-A-11-310402

本発明においては、従来の水蒸気改質器における以上の問題を解決することを目的とするものである。本発明は、改質触媒層、ＣＯ変成触媒層、ＣＯ除去触媒層のうち、特にＣＯ除去触媒層を特定の配置にして、コンパクト且つ高効率な水蒸気改質器とし、併せてその作製上、部品点数を少なく、断熱材や配管施工などの手間を少なくして、製作コストの低減を図ってなる水蒸気改質器を提供することを目的とする。 The object of the present invention is to solve the above problems in conventional steam reformers. In the present invention, among the reforming catalyst layer, the CO conversion catalyst layer, and the CO removal catalyst layer, in particular, the CO removal catalyst layer is arranged in a specific manner to form a compact and highly efficient steam reformer. An object of the present invention is to provide a steam reformer that has a reduced number of parts, reduces the labor of heat insulation and piping construction, and reduces the manufacturing cost.

本発明は、円筒状容器内に、その軸方向にガスが流通する改質触媒部、ＣＯ変成触媒部及びＣＯ除去触媒部をそれぞれ別層に区画して配置して一体化してなる炭化水素系燃料の水蒸気改質器であって、前記ＣＯ除去触媒部を円筒状容器の軸方向に平行な円筒状隔壁により一段目のＣＯ除去触媒部と二段目のＣＯ除去触媒部に区画し、一段目のＣＯ除去触媒部の出口から二段目のＣＯ除去触媒部の入口に折り返すガス流路を備えてなることを特徴とする水蒸気改質器である。 The present invention relates to a hydrocarbon system in which a reforming catalyst portion, a CO shift catalyst portion, and a CO removal catalyst portion in which a gas flows in the axial direction in a cylindrical container are arranged separately in separate layers. A steam reformer for fuel, wherein the CO removal catalyst part is partitioned into a first stage CO removal catalyst part and a second stage CO removal catalyst part by a cylindrical partition parallel to the axial direction of the cylindrical vessel. A steam reformer comprising a gas flow path that turns back from an outlet of a second CO removal catalyst section to an inlet of a second-stage CO removal catalyst section.

本水蒸気改質器は、ＣＯ除去触媒部を円筒状容器の軸方向に平行な円筒状隔壁により一段目のＣＯ除去触媒部と二段目のＣＯ除去触媒部に区画し、一段目のＣＯ除去触媒部の出口から二段目のＣＯ除去触媒部に折り返すガス流路を備えたことにより、コンパクト且つ高効率な水蒸気改質器とすることができ、信頼性を確保することができる。併せて、その作製上、部品点数を少なく、断熱材や配管施工などの手間を少なくして、製作コストの低減を図ることができる。 In this steam reformer, the CO removal catalyst part is divided into a first stage CO removal catalyst part and a second stage CO removal catalyst part by a cylindrical partition parallel to the axial direction of the cylindrical vessel, and the first stage CO removal. By providing the gas flow path that turns back from the outlet of the catalyst unit to the second-stage CO removal catalyst unit, a compact and highly efficient steam reformer can be obtained, and reliability can be ensured. In addition, the production cost can be reduced by reducing the number of parts and reducing the work such as heat insulation and piping work.

本発明は、円筒状容器内に、その軸方向にガスが流通する改質触媒部、ＣＯ変成触媒部及びＣＯ除去触媒部をそれぞれ別層に区画して配置して一体化してなる炭化水素系燃料の水蒸気改質器である。そして、前記ＣＯ除去触媒部を円筒状容器の軸方向に平行な円筒状隔壁により一段目の触媒部と二段目の触媒部に区画し、一段目のＣＯ除去触媒部の出口から二段目のＣＯ除去触媒部に折り返すガス流路を備えてなることを特徴とする。 The present invention relates to a hydrocarbon system in which a reforming catalyst portion, a CO shift catalyst portion, and a CO removal catalyst portion in which a gas flows in the axial direction in a cylindrical container are arranged separately in separate layers. This is a fuel steam reformer. The CO removal catalyst part is partitioned into a first stage catalyst part and a second stage catalyst part by a cylindrical partition parallel to the axial direction of the cylindrical container, and the second stage from the outlet of the first stage CO removal catalyst part. The CO removal catalyst part is provided with a gas flow path that turns back.

本発明の水蒸気改質器においては、上記特徴点に加え、ＣＯ除去触媒部に冷却機構を配置する。冷却機構は、（１）一段目のＣＯ除去触媒部の内壁に配置してもよく、（２）一段目のＣＯ除去触媒部の外壁に配置してもよく、（３）二段目のＣＯ除去触媒部の外壁に配置してもよく、（４）一段目のＣＯ除去触媒部の外壁と二段目のＣＯ除去触媒部への折り返し部に配置してもよく、（５）これら（１）〜（４）のいずれか二箇所以上に配置してもよい。 In the steam reformer of the present invention, in addition to the above feature points, a cooling mechanism is disposed in the CO removal catalyst unit. The cooling mechanism may be (1) disposed on the inner wall of the first stage CO removal catalyst section, (2) may be disposed on the outer wall of the first stage CO removal catalyst section, or (3) the second stage CO removal catalyst section. It may be arranged on the outer wall of the removal catalyst part, (4) it may be arranged on the outer wall of the first stage CO removal catalyst part and the folded part to the second stage CO removal catalyst part, (5) these (1 ) To (4) any two or more locations.

以下、本発明を順次説明する。図５〜１４は本発明の態様例を説明する図で、前述図１〜４と共通する部分については同じ符号を付している。図６は、図５中ＣＯ除去触媒部を含む部分を取り出し拡大して示した図である。 Hereinafter, the present invention will be described sequentially. FIGS. 5 to 14 are diagrams for explaining exemplary embodiments of the present invention, and the same reference numerals are given to portions common to FIGS. FIG. 6 is an enlarged view showing a portion including the CO removal catalyst portion in FIG.

図５〜６において、５１は一段目のＣＯ除去触媒部、５２は二段目のＣＯ除去触媒部であり、両部は円筒状容器の軸方向に平行に配置された円筒状隔壁５３により区画されている。一段目のＣＯ除去触媒部５１は第２の円筒体２と円筒状隔壁５３により区画され、二段目のＣＯ除去触媒部５２は円筒状隔壁５３と円筒状隔壁５４により区画されている。円筒状隔壁５４は、円筒体２４と同径で、その上部に配置されている。円筒状隔壁５３は、第２円筒体２の径より大きく、円筒状隔壁５４の径より小さく、円筒状容器の軸方向に対して平行ないし実質的に平行に配置されていればよく、平行とはこの意味である。 5-6, 51 is a first-stage CO removal catalyst part, 52 is a second-stage CO removal catalyst part, and both parts are partitioned by a cylindrical partition wall 53 arranged in parallel to the axial direction of the cylindrical container. Has been. The first-stage CO removal catalyst section 51 is partitioned by the second cylindrical body 2 and the cylindrical partition wall 53, and the second-stage CO removal catalyst section 52 is partitioned by the cylindrical partition wall 53 and the cylindrical partition wall 54. The cylindrical partition wall 54 has the same diameter as the cylindrical body 24 and is disposed on the upper part thereof. The cylindrical partition wall 53 may be larger than the diameter of the second cylindrical body 2 and smaller than the diameter of the cylindrical partition wall 54 and may be arranged in parallel or substantially parallel to the axial direction of the cylindrical container. Means this.

５５はＣＯ除去触媒部の下部隔壁で、支持板２２との間に間隔を置いて配置され、二段目のＣＯ除去触媒部５２の下部隔壁６２の下部まで延びている。下部隔壁５５は、第２円筒体２の径に相当する部分は第２円筒体２で占められるのでドーナツ状の隔壁である。下部隔壁５５には一つの連通孔５６が設けてあり、連通孔５６は混合分配部５７に臨ませてある。混合分配部５７は、断面Ｌ字状（図では断面逆Ｌ字状）部材５８と円筒状隔壁５３と下部隔壁５５により、円筒状隔壁５３の下部周りに形成されており、円筒状隔壁５３の下部周りには複数の透孔５９が穿設されている。 Reference numeral 55 denotes a lower partition wall of the CO removal catalyst unit, which is disposed at a distance from the support plate 22 and extends to the lower part of the lower partition wall 62 of the second stage CO removal catalyst unit 52. The lower partition 55 is a donut-shaped partition because a portion corresponding to the diameter of the second cylindrical body 2 is occupied by the second cylindrical body 2. One communication hole 56 is provided in the lower partition wall 55, and the communication hole 56 faces the mixing / distributing portion 57. The mixing / distributing portion 57 is formed around the lower portion of the cylindrical partition wall 53 by a member 58, a cylindrical partition wall 53, and a lower partition wall 55. A plurality of through holes 59 are formed around the lower portion.

支持板２２と下部隔壁５５との間の空隙に空気の供給管２９を通してＣＯ除去用空気が供給される。連通孔５６を、所定の孔径で且つ一つとすることにより、改質ガスとＣＯ除去用空気が連通孔５６を通過して混合分配部５７に流入する際に所定の通過速度が得られ、通過時の乱流により改質ガスとＣＯ除去用空気を良好に混合することができる。 CO removal air is supplied to the gap between the support plate 22 and the lower partition wall 55 through the air supply pipe 29. By using one communication hole 56 with a predetermined hole diameter, when the reformed gas and the CO removal air pass through the communication hole 56 and flow into the mixing / distributing portion 57, a predetermined passage speed can be obtained and passed. Due to the turbulent flow, the reformed gas and the CO removal air can be mixed well.

６０はＣＯ除去触媒部の上部隔壁（第２円筒体２の径に相当する部分は第２円筒体２で占められるのでドーナツ状の隔壁である）であり、ガス流通用の複数の孔６１を有する。上部隔壁６０は、二段目のＣＯ除去触媒部５２の上部隔壁でもあり、一段目のＣＯ除去触媒部５１及び二段目のＣＯ除去触媒部５２に共通する隔壁である。一段目のＣＯ除去触媒部５１側及び二段目のＣＯ除去触媒部５２側にそれぞれ複数の孔を有する上部隔壁６０と、隔壁１０と、第２円筒体２と、円筒状隔壁５４とで囲まれた空間が一段目のＣＯ除去触媒部５１の出口から二段目のＣＯ除去触媒部５２の入口に折り返すガス流路となる。６２は二段目のＣＯ除去触媒部５２の下部隔壁（円筒状隔壁５３の径に相当する部分は円筒状隔壁５３で占められるのでドーナツ状の隔壁である）であり、ガス流出用の複数の孔６３を有する。 Reference numeral 60 denotes an upper partition wall of the CO removal catalyst section (a portion corresponding to the diameter of the second cylindrical body 2 is occupied by the second cylindrical body 2 and is a donut-shaped partition wall), and has a plurality of holes 61 for gas circulation. Have. The upper partition wall 60 is also an upper partition wall of the second stage CO removal catalyst unit 52, and is a partition wall common to the first stage CO removal catalyst unit 51 and the second stage CO removal catalyst unit 52. Surrounded by the upper partition wall 60 having a plurality of holes on the first stage CO removal catalyst unit 51 side and the second stage CO removal catalyst unit 52 side, the partition wall 10, the second cylindrical body 2, and the cylindrical partition wall 54. This space becomes a gas flow path that turns back from the outlet of the first-stage CO removal catalyst section 51 to the inlet of the second-stage CO removal catalyst section 52. Reference numeral 62 denotes a lower partition wall of the second-stage CO removal catalyst unit 52 (a portion corresponding to the diameter of the cylindrical partition wall 53 is occupied by the cylindrical partition wall 53, and is a donut-shaped partition wall). A hole 63 is provided.

ＣＯ除去用空気を混合した改質ガスは混合分配部５７に穿設された複数の透孔５９を介して一段目のＣＯ除去触媒部５１に導入され、ＣＯ除去触媒上でＣＯが酸化される。その後、一段目のＣＯ除去触媒部５１側の上部隔壁６０の孔６１を経て、上部隔壁６０と隔壁１０との空隙に流れ込み、図５〜６中矢印（点線矢印）のように折り返して、二段目のＣＯ除去触媒部５２側の上部隔壁６０の孔６１を経て、二段目のＣＯ除去触媒部５２に導入される。二段目のＣＯ除去触媒部５２に導入された改質ガス中のＣＯは、ＣＯ除去触媒上でさらに酸化され、下部隔壁６２の複数の孔６３を経て改質ガス導出管６４から導出される。 The reformed gas mixed with the CO removal air is introduced into the first-stage CO removal catalyst portion 51 through a plurality of through holes 59 formed in the mixing / distributing portion 57, and CO is oxidized on the CO removal catalyst. . Thereafter, the gas flows into the gap between the upper partition wall 60 and the partition wall 10 through the hole 61 of the upper partition wall 60 on the first CO removal catalyst unit 51 side, and is folded back as indicated by an arrow (dotted line arrow) in FIGS. The gas is introduced into the second-stage CO removal catalyst section 52 through the hole 61 of the upper partition wall 60 on the second-stage CO removal catalyst section 52 side. The CO in the reformed gas introduced into the second-stage CO removal catalyst unit 52 is further oxidized on the CO removal catalyst, and is led out from the reformed gas outlet pipe 64 through the plurality of holes 63 of the lower partition wall 62. .

前述図３との対比で言えば、図３のＣＯ除去触媒部４１が、図５〜６における一段目のＣＯ除去触媒部５１に相当し、図３のＣＯ除去触媒部４２が、図５〜６における一段目のＣＯ除去触媒部５２に相当している。そして、図５〜６の二段目のＣＯ除去触媒部５２が、一段目のＣＯ除去触媒部５１の外周に配置され、円筒体２４と同径の円筒状隔壁５４で区画されていることから、外周面積をコンパクト化できる。これにより、熱エネルギーの損失を防ぎ、家庭用コージェネレーションシステムなどで使用する場合、設置スペースの制約に応えることができる。 In comparison with FIG. 3 described above, the CO removal catalyst unit 41 in FIG. 3 corresponds to the first stage CO removal catalyst unit 51 in FIGS. 5 to 6, and the CO removal catalyst unit 42 in FIG. 6 corresponds to the first-stage CO removal catalyst unit 52 in FIG. The second-stage CO removal catalyst section 52 of FIGS. 5 to 6 is disposed on the outer periphery of the first-stage CO removal catalyst section 51, and is partitioned by a cylindrical partition wall 54 having the same diameter as the cylindrical body 24. The outer peripheral area can be made compact. Thereby, the loss of heat energy is prevented, and when used in a home cogeneration system or the like, it is possible to meet the restrictions on the installation space.

本発明の水蒸気改質器は、以上の構成により、以下（ａ）〜（ｃ）の効果が達成されることが確認された。これらは、水蒸気改質器の実用化に向けての研究開発の結果として達成し得たものであり、実機水蒸気改質器において非常に有用な効果である。
（ａ）本体直径２００ｍｍの水蒸気改質器の軸方向高さを、改良前のものである図４に示す水蒸気改質器（同じく本体直径２００ｍｍ）の軸方向高さ６４０ｍｍに対して５８０ｍｍに小型化することができた。
（ｂ）本体直径２００ｍｍの水蒸気改質器の外表面積を、図４に示す示す水蒸気改質器（同じく本体直径２００ｍｍ）の外表面積に対して８％分低減できた。これにより、放熱損失を低減することができた。
（ｃ）本体直径２００ｍｍの水蒸気改質器は、図４に示す示す水蒸気改質器（同じ本体直径２００ｍｍ）に対して、本体外形（すなわち側周面）の凹凸が少なくなったため、外装の断熱材施工にかかるコストを低減することができた。 The steam reformer of the present invention was confirmed to achieve the following effects (a) to (c) with the above configuration. These can be achieved as a result of research and development for practical application of the steam reformer, and are very useful effects in the actual steam reformer.
(A) The axial height of the steam reformer having a main body diameter of 200 mm is reduced to 580 mm with respect to the axial height of 640 mm of the steam reformer (also the main body diameter of 200 mm) shown in FIG. I was able to.
(B) The outer surface area of the steam reformer having a main body diameter of 200 mm could be reduced by 8% with respect to the outer surface area of the steam reformer shown in FIG. 4 (also the main body diameter of 200 mm). Thereby, the heat dissipation loss could be reduced.
(C) The steam reformer having a main body diameter of 200 mm has less irregularities on the outer shape of the main body (that is, the side peripheral surface) than the steam reformer shown in FIG. The cost for material construction could be reduced.

〈冷却機構の配置態様１：一段目のＣＯ除去触媒部の内壁に冷却機構を配置する態様〉
図７は、本発明において一段目のＣＯ除去触媒部の内壁に冷却機構を配置する態様を説明する図である。図７において、一段目のＣＯ除去触媒部５１の内壁に冷却機構を配置した点以外は図５〜６と同様である。図７中“一段目内壁冷却機構”として示すように、一段目のＣＯ除去触媒部５１の内壁に冷却機構の冷却管７１を配置する。図７（ｂ）はその冷却管７１を取り出して示した図で、この冷却管７１がＣＯ除去触媒部の内壁に直接螺旋状に巻き付けてある。 <Arrangement Mode of Cooling Mechanism 1: Aspect of Arranging Cooling Mechanism on Inner Wall of First Stage CO Removal Catalyst Unit>
FIG. 7 is a diagram for explaining a mode in which a cooling mechanism is arranged on the inner wall of the first-stage CO removal catalyst unit in the present invention. In FIG. 7, it is the same as that of FIGS. 5-6 except the point which has arrange | positioned the cooling mechanism in the inner wall of the CO removal catalyst part 51 of the 1st step. As shown as “first stage inner wall cooling mechanism” in FIG. 7, a cooling pipe 71 of the cooling mechanism is arranged on the inner wall of the first stage CO removal catalyst unit 51. FIG. 7B is a view showing the cooling pipe 71 taken out. The cooling pipe 71 is directly spirally wound around the inner wall of the CO removal catalyst section.

冷却管７１へ供給する冷媒としては、水供給管２５または伝熱管２６中を流れる水を分岐して供給してもよく、それとは別個に水等の冷媒を供給してもよい。伝熱管２６中を流れる水を分岐して供給する場合、分岐水を図７（ａ）中ａとして示す伝熱管２６の部分から分岐して、図７（ｂ）中ｂとして示す部位に流通させる。そして、図７（ｂ）中ｃとして示す部位から、伝熱管２６の部分である図７（ａ）中ｄの部位に流通させる。本発明においては、このようにしてＣＯ除去触媒部５１におけるＣＯの酸化反応による過熱を抑えることができる。“一段目内壁冷却機構”は、冷却管７１とは限らず、ＣＯの酸化反応による過熱を抑える目的を達成し得る構造であればよく、例えば面状の冷媒流路を有する冷却機構などを用いることもできる。なお、この態様では、冷却管７１が無くとも、原料ガスと水蒸気の混合ガスが流れる流路１４を冷却機構とすることもできる。 As a refrigerant to be supplied to the cooling pipe 71, water flowing in the water supply pipe 25 or the heat transfer pipe 26 may be branched and supplied, or a refrigerant such as water may be supplied separately. When the water flowing through the heat transfer tube 26 is branched and supplied, the branched water is branched from the portion of the heat transfer tube 26 shown as a in FIG. 7A and circulated to the site shown as b in FIG. 7B. . And it distribute | circulates from the site | part shown as c in FIG.7 (b) to the site | part of FIG.7 (a) which is a part of the heat exchanger tube 26. FIG. In the present invention, overheating due to the oxidation reaction of CO in the CO removal catalyst unit 51 can be suppressed in this way. The “first-stage inner wall cooling mechanism” is not limited to the cooling pipe 71 and may be any structure that can achieve the purpose of suppressing overheating due to the oxidation reaction of CO. For example, a cooling mechanism having a planar refrigerant flow path is used. You can also In this embodiment, even if there is no cooling pipe 71, the flow path 14 through which the mixed gas of the source gas and water vapor flows can be used as the cooling mechanism.

〈冷却機構の配置態様２：一段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様〉
図８は、本発明において一段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様を説明する図である。図８において、一段目のＣＯ除去触媒部５１の外壁５３に冷却機構を配置した点以外は図５〜６と同様である。図８中“一段目外壁冷却機構”として示すように、一段目のＣＯ除去触媒部５１の外壁に冷却機構の冷却管７２を配置する。図８（ｂ）はその冷却管７２を取り出して示した図で、この冷却管７２がＣＯ除去触媒部の内壁に直接螺旋状に巻き付けてある。 <Arrangement mode 2 of cooling mechanism: A mode in which the cooling mechanism is arranged on the outer wall of the first stage CO removal catalyst unit>
FIG. 8 is a diagram for explaining a mode in which a cooling mechanism is arranged on the outer wall of the first-stage CO removal catalyst unit in the present invention. In FIG. 8, it is the same as that of FIGS. 5-6 except the point which has arrange | positioned the cooling mechanism in the outer wall 53 of the CO removal catalyst part 51 of the 1st step | paragraph. As shown as “first stage outer wall cooling mechanism” in FIG. 8, a cooling pipe 72 of the cooling mechanism is arranged on the outer wall of the first stage CO removal catalyst unit 51. FIG. 8B is a view showing the cooling pipe 72 taken out. The cooling pipe 72 is directly spirally wound around the inner wall of the CO removal catalyst section.

冷却管７２へ供給する冷媒としては、水供給管２５または伝熱管２６中を流れる水を供給してもよく、それとは別個に水等の冷媒を供給してもよい。伝熱管２６を流れる水を供給する場合、図８（ａ）に示すように、伝熱管２６を冷却管７２に連結することで行うことができる。本発明においては、このようにして、ＣＯ除去触媒部５１におけるＣＯの酸化反応による過熱を抑えることができる。“一段目外壁冷却機構”は、冷却管７２とは限らず、ＣＯの酸化反応による過熱を抑える目的を達成し得る構造であればよく、例えば面状の冷媒流路を有する冷却機構などを用いることもできる。 As a refrigerant to be supplied to the cooling pipe 72, water flowing through the water supply pipe 25 or the heat transfer pipe 26 may be supplied, or a refrigerant such as water may be supplied separately from the water. When supplying the water which flows through the heat exchanger tube 26, it can carry out by connecting the heat exchanger tube 26 to the cooling tube 72, as shown to Fig.8 (a). In the present invention, overheating due to the oxidation reaction of CO in the CO removal catalyst unit 51 can be suppressed in this way. The “first-stage outer wall cooling mechanism” is not limited to the cooling pipe 72 and may be any structure that can achieve the purpose of suppressing overheating due to the oxidation reaction of CO. For example, a cooling mechanism having a planar refrigerant flow path is used. You can also

〈冷却機構の配置態様３：二段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様〉
図９は、本発明において二段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様を説明する図である。なお、図９は後述冷〈却機構の配置態様４〉の説明図でもある。図９において、二段目のＣＯ除去触媒部５２の外壁５４に冷却機構を配置した点以外は図７と同様である。図９中“二段目外壁冷却機構”として示すように、二段目のＣＯ除去触媒部５２の外壁に冷却機構の冷却管７３を配置する。なお、この態様では、伝熱管２６そのものを冷却管７３として用いたものに相当している。 <Arrangement mode 3 of cooling mechanism: A mode in which the cooling mechanism is arranged on the outer wall of the second stage CO removal catalyst unit>
FIG. 9 is a diagram illustrating a mode in which a cooling mechanism is arranged on the outer wall of the second stage CO removal catalyst unit in the present invention. FIG. 9 is also an explanatory diagram of a cooling <disposition mechanism arrangement mode 4> described later. 9 is the same as FIG. 7 except that a cooling mechanism is arranged on the outer wall 54 of the second-stage CO removal catalyst unit 52. As shown as “second-stage outer wall cooling mechanism” in FIG. 9, a cooling pipe 73 of the cooling mechanism is arranged on the outer wall of the second-stage CO removal catalyst unit 52. In this aspect, the heat transfer tube 26 itself corresponds to the cooling tube 73.

図９（ｂ）はその冷却管７３を取り出して示した図で、この冷却管７３がＣＯ除去触媒部の外壁５４に直接螺旋状に巻き付けてある。図９の態様では、冷却管７３へ供給する冷媒は、伝熱管２６中を流れる水である。伝熱管２６を流れる水は、冷却管７３中を流通した後、混合部１３で原料ガスに混合される。本発明においては、このようにして、ＣＯ除去触媒部５２におけるＣＯの酸化反応による過熱を抑えることができる。“二段目外壁冷却機構”は、冷却管７３とは限らず、ＣＯの酸化反応による過熱を抑える目的を達成し得る構造であればよく、例えば面状の冷媒流路を有する形式などを用いることもできる。 FIG. 9B shows the cooling pipe 73 taken out. The cooling pipe 73 is directly spirally wound around the outer wall 54 of the CO removal catalyst section. In the aspect of FIG. 9, the refrigerant supplied to the cooling pipe 73 is water flowing through the heat transfer pipe 26. The water flowing through the heat transfer tube 26 flows through the cooling tube 73 and then mixed with the raw material gas in the mixing unit 13. In the present invention, overheating due to the oxidation reaction of CO in the CO removal catalyst unit 52 can be suppressed in this way. The “second-stage outer wall cooling mechanism” is not limited to the cooling pipe 73 and may have any structure that can achieve the purpose of suppressing overheating due to the oxidation reaction of CO. For example, a type having a planar refrigerant flow path is used. You can also

〈冷却機構の配置態様４：一段目のＣＯ除去触媒部の内壁に冷却機構を配置し、且つ、二段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様〉
図９は、本発明において一段目のＣＯ除去触媒部の内壁に冷却機構を配置し、且つ、二段目のＣＯ除去触媒部の外壁に冷却機構を配置する態様を説明する図である。図９中、“一段目内壁冷却機構”、“二段目外壁冷却機構”として示すように冷却機構を二箇所に設ける。このうち“一段目内壁冷却機構”の態様については前述〈冷却機構の配置態様１〉と同様であり、“二段目外壁冷却機構”の態様については前述〈冷却機構の配置態様３〉と同様である。本発明においては、このようにして、ＣＯ除去触媒部５１、５２におけるＣＯの酸化反応による過熱を抑えることができる。 <Cooling Mechanism Arrangement Mode 4: Mode in which the cooling mechanism is disposed on the inner wall of the first-stage CO removal catalyst unit, and the cooling mechanism is disposed on the outer wall of the second-stage CO removal catalyst unit>
FIG. 9 is a diagram for explaining a mode in which a cooling mechanism is arranged on the inner wall of the first-stage CO removal catalyst unit and a cooling mechanism is arranged on the outer wall of the second-stage CO removal catalyst unit in the present invention. In FIG. 9, two cooling mechanisms are provided as shown as “first-stage inner wall cooling mechanism” and “second-stage outer wall cooling mechanism”. Among these, the aspect of the “first-stage inner wall cooling mechanism” is the same as the above-mentioned <cooling mechanism arrangement aspect 1>, and the aspect of the “second-stage outer wall cooling mechanism” is the same as the above-mentioned <cooling mechanism arrangement aspect 3>. It is. In the present invention, overheating due to the oxidation reaction of CO in the CO removal catalyst units 51 and 52 can be suppressed in this way.

〈冷却機構の配置態様５：一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部への折り返し部に冷却機構を配置する態様〉
図１０〜１１は、本発明において一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部への折り返し部に冷却機構を配置する態様を説明する図である。図１０において、一段目のＣＯ除去触媒部５１から二段目のＣＯ除去触媒部５２への折り返し部に冷却機構を配置した点以外は図５〜６と同様である。図１０中“折返部冷却機構”として示すように、一段目のＣＯ除去触媒部５１から二段目のＣＯ除去触媒部５２へのガスの折り返し部に冷却機構の冷却管７５を配置する。 <Arrangement Mode 5 of Cooling Mechanism: Aspect in which Cooling Mechanism is Arranged at the Folded Portion from the First Stage CO Removal Catalyst Part to the Second Stage CO Removal Catalyst Part>
FIGS. 10-11 is a figure explaining the aspect which arrange | positions a cooling mechanism in the folding | turning part from the CO removal catalyst part of the 1st step to the CO removal catalyst part of the 2nd step in this invention. 10 is the same as FIGS. 5 to 6 except that a cooling mechanism is arranged at the folded portion from the first-stage CO removal catalyst section 51 to the second-stage CO removal catalyst section 52. As shown as “turning part cooling mechanism” in FIG. 10, the cooling pipe 75 of the cooling mechanism is arranged at the gas turning part from the first stage CO removal catalyst part 51 to the second stage CO removal catalyst part 52.

図１１はその冷却管７５を取り出して示して平面図として示した図である。図１１のとおり、この冷却管７５が一段目のＣＯ除去触媒部５１から二段目のＣＯ除去触媒部５２への折り返し部に配置してある。冷媒は、導入管７４から供給され、導出管７６から排出される。図１０〜１１の態様では、冷却管７５へ供給する冷媒としては、水供給管２５または伝熱管２６中を流れる水を分岐して供給してもよく、それとは別個に水等の冷媒を供給してもよい。本発明においては、このようにして、ＣＯ除去触媒部５１、５２におけるＣＯの酸化反応による過熱を抑えることができる。“折返部冷却機構”は、冷却管７５とは限らず、ＣＯの酸化反応による過熱を抑える目的を達成し得る構造であればよく、例えば面状の冷媒流路を有する冷却機構などとしてもよい。 FIG. 11 shows the cooling pipe 75 taken out and shown as a plan view. As shown in FIG. 11, the cooling pipe 75 is arranged at the turn-back portion from the first-stage CO removal catalyst section 51 to the second-stage CO removal catalyst section 52. The refrigerant is supplied from the introduction pipe 74 and discharged from the outlet pipe 76. 10 to 11, as the refrigerant to be supplied to the cooling pipe 75, water flowing in the water supply pipe 25 or the heat transfer pipe 26 may be branched and supplied, and separately, a refrigerant such as water is supplied. May be. In the present invention, overheating due to the oxidation reaction of CO in the CO removal catalyst units 51 and 52 can be suppressed in this way. The “folding portion cooling mechanism” is not limited to the cooling pipe 75, and may be any structure that can achieve the purpose of suppressing overheating due to the oxidation reaction of CO. For example, a cooling mechanism having a planar refrigerant flow path may be used. .

〈一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部へのガス折り返し部にＣＯ除去用空気と改質ガスの混合機構を配置した態様（その１）〉
図１２〜１３は、本発明の水蒸気改質器において、一段目のＣＯ除去触媒部と二段目ののＣＯ除去触媒部５１の折り返し部にＣＯ除去用空気と改質ガスとの混合機構を配置した態様を説明する図である。図１２において、この混合機構を配置した点以外は図５〜６と同様である。図１２中“折返部空気混合機構”として示すように、一段目のＣＯ除去触媒部５１から二段目のＣＯ除去触媒部５２への改質ガスの折り返し部にＣＯ除去用空気と改質ガスとの混合機構を配置する。８１は空気の分配管である。 <Aspect (No. 1) in which a mechanism for mixing CO-removing air and reformed gas is disposed at the gas turn-back portion from the first-stage CO removal catalyst section to the second-stage CO removal catalyst section>
12 to 13 show a steam reformer according to the present invention, in which the mixing mechanism of the CO removal air and the reformed gas is provided at the folded portion of the first-stage CO removal catalyst section and the second-stage CO removal catalyst section 51. It is a figure explaining the arrange | positioned aspect. In FIG. 12, it is the same as that of FIGS. 5-6 except the point which has arrange | positioned this mixing mechanism. As shown as “turning part air mixing mechanism” in FIG. 12, the CO removal air and the reformed gas are supplied to the return part of the reformed gas from the first stage CO removal catalyst part 51 to the second stage CO removal catalyst part 52. And arrange the mixing mechanism. Reference numeral 81 denotes an air distribution pipe.

図１３はその空気分配管８１を取り出して示して平面図として示した図である。図１３（ａ）において、８０は空気分配管８１への空気供給管、８２は空気放出用の孔で、複数の孔８２が間隔を置いて穿設してある。空気は、導入管８０から空気分配管８１へ供給され、複数の孔８２から放出される。折り返し部には一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部５２へ改質ガスが流れているので、改質ガスが放出空気と混合する。これにより改質ガスの確実なＣＯ低減が行える。 FIG. 13 shows the air distribution pipe 81 taken out and shown as a plan view. In FIG. 13A, 80 is an air supply pipe to the air distribution pipe 81, 82 is a hole for air discharge, and a plurality of holes 82 are formed at intervals. Air is supplied from the introduction pipe 80 to the air distribution pipe 81 and discharged from the plurality of holes 82. Since the reformed gas flows from the first-stage CO removal catalyst section to the second-stage CO removal catalyst section 52 in the folding section, the reformed gas mixes with the released air. As a result, the CO of the reformed gas can be reliably reduced.

分配管８１は、図１３（ａ）に示すような断面円環状のほか、断面４角形状、断面３角形状、断面楕円形状など各種態様に構成することができる。孔８２は、分配管８１について、その断面で見て上側、下側、上下両側、側面側、斜め側、あるいは、それらのうち複数の各側に規則的または不規則に穿設するなど、改質ガスへの空気の混合目的を達成し得る各種態様で穿設することができる。図１３（ｂ）は、そのうち断面円環状の分配管８１の外側面側に複数の孔８２を穿設した態様を示す図である。 The distribution pipe 81 can be configured in various forms such as a cross-section annular shape as shown in FIG. The holes 82 are modified in such a manner that the distribution pipe 81 is perforated on the upper side, the lower side, the upper and lower sides, the side surface side, the oblique side, or a plurality of them regularly or irregularly. It can be drilled in various ways that can achieve the purpose of mixing the air with the quality gas. FIG. 13B is a view showing an aspect in which a plurality of holes 82 are formed on the outer surface side of the distribution pipe 81 having an annular cross section.

〈一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部へのガス折り返し部にＣＯ除去用空気と改質ガスの混合機構を配置した態様（その２）〉
図１４は、本発明の水蒸気改質器において、一段目のＣＯ除去触媒部と二段目のＣＯ除去触媒部５１の折り返し部にＣＯ除去用空気と改質ガスとの混合機構を配置した他の態様を説明する図である。図１４において、混合機構を配置した点以外は図５〜６と同様である。図１４（ｂ）は、図１４（ａ）の混合機構を含む部分を拡大して示した図である。 <Aspect (No. 2) in which a mechanism for mixing CO-removing air and reformed gas is disposed at the gas turn-back portion from the first-stage CO removal catalyst section to the second-stage CO removal catalyst section>
FIG. 14 shows a steam reformer according to the present invention in which a mechanism for mixing CO-removing air and reformed gas is disposed at the folded portion of the first-stage CO removal catalyst section and the second-stage CO removal catalyst section 51. It is a figure explaining the aspect of. In FIG. 14, it is the same as that of FIGS. 5-6 except the point which has arrange | positioned the mixing mechanism. FIG. 14B is an enlarged view showing a portion including the mixing mechanism of FIG.

図１４のとおり、隔壁１０とＣＯ除去触媒部の上部隔壁６０との間の空隙にＣＯ除去用空気の供給管８０の供給口を臨ませる。上部隔壁６０は、一段目のＣＯ除去触媒部５１の部分はガス流通用の複数の孔６１を有し、二段目のＣＯ除去触媒部５２の部分は導入管８０の位置と相対する側に一つの連通孔９３を有する。二段目のＣＯ除去触媒部５２の部分に対応する上部隔壁６０の下部に、間隔を置いてガス流通用の複数の孔９２を有する隔壁９１を配置する。隔壁９１は、円筒状隔壁５３の径に相当する部分は円筒状隔壁５３で占められるのでドーナツ状の隔壁である。 As shown in FIG. 14, the supply port of the CO removal air supply pipe 80 faces the gap between the partition wall 10 and the upper partition wall 60 of the CO removal catalyst unit. In the upper partition wall 60, the first stage CO removal catalyst part 51 has a plurality of gas flow holes 61, and the second stage CO removal catalyst part 52 part is on the side opposite to the position of the introduction pipe 80. One communication hole 93 is provided. A partition wall 91 having a plurality of gas flow holes 92 is arranged at intervals below the upper partition wall 60 corresponding to the second-stage CO removal catalyst unit 52. The partition 91 is a donut-shaped partition because a portion corresponding to the diameter of the cylindrical partition 53 is occupied by the cylindrical partition 53.

図１４（ｂ）中、１点鎖線はＣＯ除去用空気の流れを示し、点線は一段目のＣＯ除去触媒部５１からの改質ガスの流れを示し、実線は改質ガスとＣＯ除去用空気の混合ガスの流れを示している。ＣＯ除去用空気が、その供給管８０を通して隔壁１０と上部隔壁６０との間の空隙に供給される。ＣＯ除去用空気は円筒状隔壁５３の外周に沿って湾曲しながら、一段目のＣＯ除去触媒部５１からの改質ガスと混合し、連通孔９３を通過する時の乱流によりさらに混合される。混合ガスは、隔壁９１の複数の孔９２を経て二段目のＣＯ除去触媒部５２に流入してさらにＣＯが酸化低減され、下部隔壁６２のガス流出用の複数の孔６３を経て改質ガス導出管６４から導出される。 In FIG. 14B, the alternate long and short dash line indicates the flow of the CO removal air, the dotted line indicates the flow of the reformed gas from the first stage CO removal catalyst unit 51, and the solid line indicates the reformed gas and the CO removal air. The flow of the mixed gas is shown. The CO removing air is supplied to the gap between the partition wall 10 and the upper partition wall 60 through the supply pipe 80. The CO removal air is curved along the outer periphery of the cylindrical partition wall 53, mixed with the reformed gas from the first-stage CO removal catalyst unit 51, and further mixed by turbulent flow when passing through the communication hole 93. . The mixed gas flows into the second-stage CO removal catalyst portion 52 through the plurality of holes 92 of the partition wall 91, further reduces the oxidation of CO, and reformed gas through the plurality of gas outlet holes 63 of the lower partition wall 62. Derived from the outlet tube 64.

以上のように、一段目のＣＯ除去触媒部の出口から二段目のＣＯ除去触媒部に折り返す改質ガス流路にＣＯ除去用空気の混合機構を配置したことにより確実なＣＯ低減が行えるようになった。 As described above, the CO removal air mixing mechanism is arranged in the reformed gas flow path that is turned back from the outlet of the first stage CO removal catalyst section to the second stage CO removal catalyst section, so that reliable CO reduction can be performed. Became.

水蒸気改質器の一例（先行技術）を縦断面図として示す図The figure which shows an example (prior art) of a steam reformer as a longitudinal section 図１におけるＣＯ除去触媒層３４の部分を中心に拡大して示した図The figure which expanded and showed centering on the part of the CO removal catalyst layer 34 in FIG. 水蒸気改質器の他の例（先行技術）を縦断面図として示す図The figure which shows other examples (prior art) of a steam reformer as a longitudinal section 水蒸気改質器の他の例（先行技術）を縦断面図として示す図The figure which shows other examples (prior art) of a steam reformer as a longitudinal section 本発明の水蒸気改質器の態様例を縦断面図として示す図The figure which shows the aspect example of the steam reformer of this invention as a longitudinal cross-sectional view 図５におけるＣＯ除去触媒層の部分を中心に拡大して示した図The figure which expanded and showed centering on the part of the CO removal catalyst layer in FIG. 本発明の水蒸気改質器の他の態様例を縦断面図として示す図The figure which shows the other example of a steam reformer of this invention as a longitudinal cross-sectional view 本発明の水蒸気改質器の他の態様例を縦断面図として示す図The figure which shows the other example of a steam reformer of this invention as a longitudinal cross-sectional view 本発明の水蒸気改質器の他の態様例を縦断面図として示す図The figure which shows the other example of a steam reformer of this invention as a longitudinal cross-sectional view 本発明の水蒸気改質器の他の態様例を縦断面図として示す図The figure which shows the other example of a steam reformer of this invention as a longitudinal cross-sectional view 図１０における冷却管７５を取り出して示して示した図The figure which took out and showed the cooling pipe 75 in FIG. 一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部へのガス折り返し部にＣＯ除去用空気と改質ガスの混合機構を配置した態様（その１）を示す図The figure which shows the aspect (the 1) which has arrange | positioned the mixing mechanism of the CO removal air and reformed gas in the gas return part from the CO removal catalyst part of the 1st stage to the CO removal catalyst part of the 2nd stage. 図１２の一部を拡大して示した図FIG. 12 is an enlarged view of a part of FIG. 一段目のＣＯ除去触媒部から二段目のＣＯ除去触媒部へのガス折り返し部にＣＯ除去用空気と改質ガスの混合機構を配置した態様（その２）を示す図The figure which shows the aspect (the 2) which has arrange | positioned the mixing mechanism of the air for CO removal and reformed gas in the gas return part from the CO removal catalyst part of the 1st stage to the CO removal catalyst part of the 2nd stage.

Explanation of symbols

１〜４第１円筒体〜第４円筒体
５輻射筒
６バーナー
７上蓋兼バーナー取付台
８底板
９燃焼排ガスの排気通路
１０隔壁
２１ＣＯ変成触媒層
２２支持板
２７仕切板
２８連通孔
２９ＣＯ除去用空気供給管
３０円環状の通路
３３支持板
３４複数個の孔
３５ＣＯ除去触媒層
３６円筒体
３７支持板
４０断熱材
４１、４２ＣＯ除去触媒部
５１一段目のＣＯ除去触媒部
５２二段目のＣＯ除去触媒部
５３、５４円筒状隔壁
５５ＣＯ除去触媒部の下部隔壁
５６、９３連通孔（各一つ）
５７混合分配部
５８断面Ｌ字状（逆Ｌ字状）部材
５９透孔
６０ＣＯ除去触媒部の上部隔壁
６１ガス流通用の複数の孔
６２二段目のＣＯ除去触媒部の下部隔壁
６３下部隔壁６２の複数の孔
６４改質ガス導出管
７１一段目のＣＯ除去触媒部５１の内壁に配置した冷却管
７２一段目のＣＯ除去触媒部５１の外壁に配置した冷却管
７３二段目のＣＯ除去触媒部５２の外壁に配置した冷却管
７５一段目のＣＯ除去触媒部５１から二段目のＣＯ除去触媒部５２へのガス折り返し部に配置した冷却管
８０ＣＯ除去用空気供給管
８１空気分配管
８２複数の孔
９１隔壁
９２ガス流通用の複数の孔 1-4 1st cylinder body-4th cylinder body 5 Radiation tube 6 Burner 7 Upper lid / burner mounting base 8 Bottom plate 9 Exhaust passage for combustion exhaust gas 10 Partition wall 21 CO shift catalyst layer 22 Support plate 27 Partition plate 28 Communication hole 29 CO removal Air supply pipe 30 Annular passage 33 Support plate 34 Multiple holes 35 CO removal catalyst layer 36 Cylindrical body 37 Support plate 40 Heat insulating material 41, 42 CO removal catalyst part 51 First stage CO removal catalyst part 52 Second stage CO removal catalyst part 53, 54 Cylindrical partition wall 55 Lower partition wall of CO removal catalyst part 56, 93 Communication hole (each one)
57 Mixing / distributing portion 58 L-shaped (inverted L-shaped) member 59 Through-hole 60 Upper partition wall of CO removal catalyst portion 61 Multiple holes for gas flow 62 Lower partition wall of second-stage CO removal catalyst portion 63 Lower partition wall 62 plural holes 64 reformed gas outlet pipe 71 cooling pipe arranged on the inner wall of the first stage CO removal catalyst part 51 72 cooling pipe arranged on the outer wall of the first stage CO removal catalyst part 51 73 second stage CO removal Cooling pipe arranged on the outer wall of the catalyst part 52 75 Cooling pipe arranged in the gas turn-up part from the first-stage CO removal catalyst part 51 to the second-stage CO removal catalyst part 52 80 CO removal air supply pipe 81 Air distribution pipe 82 Multiple holes 91 Bulkhead 92 Multiple holes for gas flow

Claims

In the cylindrical container, steam reforming of the hydrocarbon-based fuel, in which the reforming catalyst part, the CO conversion catalyst part and the CO removal catalyst part in which the gas flows in the axial direction is divided and arranged in separate layers, is integrated. The CO removal catalyst section is divided into a first stage CO removal catalyst section and a second stage CO removal catalyst section by a cylindrical partition parallel to the axial direction of the cylindrical container, and the first stage CO removal A hydrocarbon fuel steam reformer comprising a gas flow path that turns back from an outlet of a catalyst section to an inlet of a second-stage CO removal catalyst section.

2. The hydrocarbon fuel steam reformer according to claim 1, wherein a cooling mechanism is disposed on an inner wall of the first stage CO removal catalyst section.

3. The hydrocarbon fuel steam reformer according to claim 1, wherein a cooling mechanism is disposed on an outer wall of the first-stage CO removal catalyst unit. 4.

The hydrocarbon fuel steam reformer according to any one of claims 1 to 3, wherein a cooling mechanism is disposed on an outer wall of the second stage CO removal catalyst section. Steam reformer.

5. The hydrocarbon fuel steam reformer according to claim 1, wherein a cooling mechanism is disposed in a gas return portion from the first-stage CO removal catalyst section to the second-stage CO removal catalyst section. A steam reformer for hydrocarbon fuel, characterized by comprising:

6. The hydrocarbon fuel steam reformer according to claim 1, wherein CO removal air is provided at a gas turn-up portion from the first-stage CO removal catalyst portion to the second-stage CO removal catalyst portion. And a reformer gas mixing mechanism, characterized in that it is a hydrocarbon fuel steam reformer.

The steam reformer for hydrocarbon fuel according to any one of claims 1 to 6, having a heating part in the center, a reforming part and a CO conversion part in the periphery thereof, and having a structure in which each is integrated. A steam reformer for hydrocarbon fuel, characterized by