JPH01183401A - Fuel reformer - Google Patents
Fuel reformerInfo
- Publication number
- JPH01183401A JPH01183401A JP453388A JP453388A JPH01183401A JP H01183401 A JPH01183401 A JP H01183401A JP 453388 A JP453388 A JP 453388A JP 453388 A JP453388 A JP 453388A JP H01183401 A JPH01183401 A JP H01183401A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- reaction
- reforming
- gas flow
- raw material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000000446 fuel Substances 0.000 title claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 75
- 238000006243 chemical reaction Methods 0.000 claims abstract description 59
- 238000002407 reforming Methods 0.000 claims abstract description 38
- 239000002994 raw material Substances 0.000 claims abstract description 23
- 239000002245 particle Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 abstract description 59
- 239000000567 combustion gas Substances 0.000 abstract description 17
- 238000006057 reforming reaction Methods 0.000 abstract description 17
- 238000010438 heat treatment Methods 0.000 abstract description 13
- 238000010521 absorption reaction Methods 0.000 abstract 1
- 238000002485 combustion reaction Methods 0.000 description 13
- 239000012495 reaction gas Substances 0.000 description 11
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000011810 insulating material Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 229910017060 Fe Cr Inorganic materials 0.000 description 1
- 229910002544 Fe-Cr Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- UPHIPHFJVNKLMR-UHFFFAOYSA-N chromium iron Chemical compound [Cr].[Fe] UPHIPHFJVNKLMR-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、アルコール類や炭化水素系燃料を水蒸気改質
して水素を生成する燃料改質装置に係わり、特に、燃料
電池システム及び水素製造装置に好適な燃料改質装置に
関する。Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a fuel reformer that generates hydrogen by steam reforming alcohol or hydrocarbon fuel, and particularly relates to a fuel cell system and hydrogen production. The present invention relates to a fuel reformer suitable for the apparatus.
従来の燃料改質装置は、時開６０−２６４３０２号に示
される如く、反応部には円筒状の反応管を使用し、改質
触媒は、反応管内部に充填されていた。さらに、改質触
媒を効率良く加熱するために１反応管内部にはスペーサ
が設けられ、環状触煤層とすることで伝熱特性の改善を
図っていた。As shown in Jikai No. 60-264302, a conventional fuel reformer uses a cylindrical reaction tube for the reaction section, and a reforming catalyst is filled inside the reaction tube. Furthermore, in order to efficiently heat the reforming catalyst, a spacer is provided inside one reaction tube to form an annular soot layer to improve heat transfer characteristics.
また１反応管を加熱するための伝熱部では、熱源となる
燃焼ガスを発生するバーナ燃焼室と燃焼ガスからの熱伝
達を促進するため、燃焼ガス流路に伝熱粒子が充填され
た伝熱層とすることや、燃焼ガスの温度低下に合わせて
流路を狭くすることにより伝熱効率の向上を図っていた
。In addition, in the heat transfer section for heating one reaction tube, in order to promote heat transfer from the burner combustion chamber that generates combustion gas as a heat source and the combustion gas, the combustion gas flow path is filled with heat transfer particles. Heat transfer efficiency was improved by creating a thermal layer and by narrowing the flow path as the temperature of the combustion gas decreased.
また、特開昭５９−２１７６０５号に示される如く、中
央部にＣＯ転化触媒層が新しく設けている従来例も存在
する。Furthermore, as shown in Japanese Patent Laid-Open No. 59-217605, there is also a conventional example in which a CO conversion catalyst layer is newly provided in the center.
上記従来技術による反応管タイプの改質装置では、構造
が比較的簡単であり、改質効率もある程度確保出来るた
め、小型化を指向する燃料電池等に使用されている。し
かし、高効率化を図るうえで、構造が複雑になる等の問
題点がある為、あまり改善がなされておらず、現在以上
の小型・コンパクト化への対応は困難であった。The reaction tube type reformer according to the above-mentioned conventional technology has a relatively simple structure and can secure a certain degree of reforming efficiency, so it is used in fuel cells and the like that are aimed at miniaturization. However, in order to achieve high efficiency, there are problems such as the structure becoming complicated, so not much improvement has been made, and it has been difficult to respond to further miniaturization and compactness.
本発明の目的は、改質反応の高効率化が可能で、さらに
小型・コンパクトな燃料改質装置を提供することにある
。An object of the present invention is to provide a small and compact fuel reformer that can improve the efficiency of the reforming reaction.
上記目的を達成するために本発明は、改質触媒が充填さ
れてなる第１のガス流通路と、該通路に原料ガスを供給
する原料ガス供給手段と、前記第１のガス流通路内の原
料ガスに熱量を付与する伝熱手段と、前記第１のガス流
通路内の原料ガスが改質された改質ガスを取り出す取り
出し手段とを備えてなる燃料改質装置において、前記第
１のガス流通路に隣接されて設けられ、内部にｃｏ転化
触媒が充填されてなる第２のガス流通路と、前記第１の
ガス流通路から出たガスが当該第２のガス流通路に導く
ための改質ガス導入部とが設けられていることを特徴と
する燃料改質装置である。In order to achieve the above object, the present invention provides a first gas flow passage filled with a reforming catalyst, a raw material gas supply means for supplying raw material gas to the passage, and a gas flow passage in the first gas flow passage. In the fuel reformer, the fuel reformer comprises a heat transfer means for imparting heat to the raw material gas, and a take-out means for taking out the reformed gas obtained by reforming the raw material gas in the first gas flow path. a second gas flow path provided adjacent to the gas flow path and filled with a co-conversion catalyst; and a second gas flow path for guiding the gas discharged from the first gas flow path to the second gas flow path. This fuel reformer is characterized in that it is provided with a reformed gas introduction section.
上記本発明によれば、改質触媒が充填された第１のガス
流通路と、ＣＯ転化触媒が充填された第２のガス流通路
とが隣接されて設けられているため、ＣＯ転化反応によ
り発生する熱を第１の通路内に充填された改質触媒層の
改質反応熱として利用することが出来る。According to the present invention, since the first gas flow passage filled with the reforming catalyst and the second gas flow passage filled with the CO conversion catalyst are provided adjacent to each other, the CO conversion reaction The generated heat can be used as reforming reaction heat of the reforming catalyst layer filled in the first passage.
改質反応は次式により示される。The reforming reaction is shown by the following equation.
ＣＨ，＋２Ｈ，Ｏ→Ｃｏ、＋４Ｈ，（吸熱反応）但し、
８００℃に於ける平衡反応では約１５％のＣＯが発生す
る。CH, +2H, O → Co, +4H, (endothermic reaction) However,
Approximately 15% CO is evolved in an equilibrium reaction at 800°C.
次に、ＣＯ転化反応は次式により示される。Next, the CO conversion reaction is shown by the following equation.
ＧＯ＋Ｈ，Ｏ→Ｃｏ、＋Ｈ，（発熱反応）ｃｏ転化触媒
層を流れる改質ガスは徐々に反応を進めながら発熱及び
顕熱を改質触媒層に与えており、かつ、改質触媒層は、
°充填層となっているため、より熱伝達が促進され、伝
熱面積の縮減が可能となり高効率で小型・コンパクトな
燃料改質装置を提供出来る。GO+H, O→Co, +H, (exothermic reaction) The reformed gas flowing through the co conversion catalyst layer gives heat and sensible heat to the reforming catalyst layer while gradually proceeding with the reaction, and the reforming catalyst layer
° Since it is a packed bed, heat transfer is further promoted and the heat transfer area can be reduced, making it possible to provide a highly efficient, small and compact fuel reformer.
以下、本発明の実施例を添付図面に基づいて説明する。 Embodiments of the present invention will be described below with reference to the accompanying drawings.
第１図は本発明の一実施例の構成を示した縦断面図であ
る。第１図において、外管１と内管３とからなる２重管
が複数配置されている。外管１と内管３の間に環状部に
は、改質触媒２が充填されて、改質触媒層１４が構成さ
れている。前記内管３の内側にはＣＯ転化触媒４が充填
されたＣＯ転化触媒層１５が設けられている。燃焼ガス
流路となる前記外管１と胴５の内側には、断熱材６が設
けられている。この断熱材６と前記外管１との間には伝
熱促進を図るため耐熱性のアルミナ球を利用した伝熱粒
子１３が充填された加熱層１６が設けられ、伝熱効率を
高めている。熱源として必要な熱量を発生させるため、
下部に燃焼装置１２が備えられている。燃焼装置として
は、一般的にはバーナが用いられているが、燃焼触媒を
用いた触媒燃焼方式としても良い。FIG. 1 is a longitudinal sectional view showing the structure of an embodiment of the present invention. In FIG. 1, a plurality of double tubes each consisting of an outer tube 1 and an inner tube 3 are arranged. The annular portion between the outer tube 1 and the inner tube 3 is filled with a reforming catalyst 2 to form a reforming catalyst layer 14 . A CO conversion catalyst layer 15 filled with a CO conversion catalyst 4 is provided inside the inner tube 3 . A heat insulating material 6 is provided inside the outer tube 1 and the shell 5, which serve as a combustion gas flow path. A heating layer 16 filled with heat transfer particles 13 made of heat-resistant alumina spheres is provided between the heat insulating material 6 and the outer tube 1 in order to promote heat transfer, thereby increasing heat transfer efficiency. In order to generate the necessary amount of heat as a heat source,
A combustion device 12 is provided at the bottom. A burner is generally used as the combustion device, but a catalytic combustion system using a combustion catalyst may also be used.
改質用の原料は、原料入ロアを通って前記改質触媒層１
４に供給される。前記改質触媒層１４に供給された原料
は、改質反応を始め徐々に水素富化ガスに改質される。The raw material for reforming passes through the raw material input lower and enters the reforming catalyst layer 1.
4. The raw material supplied to the reforming catalyst layer 14 starts a reforming reaction and is gradually reformed into hydrogen-enriched gas.
改質反応は吸熱反応であるため、前記ＣＯ転化触媒層１
５を流れる改質ガス及び前記加熱層１６を流れる燃焼ガ
スより吸熱が行なわれる６次に、改質反応の終了した改
質ガスは、前記ＣＯ転化触媒層１５へ供給され、徐々に
ＣＯ転化反応を行い、改質ガス出口８より導き出される
。改質ガスは、改質反応中のガスである反応ガスより常
に温度が高く、また、ＣＯ転化反応は発熱反応でありＪ
より多くの熱を前記改質触媒層１４へ供給できる。この
時、改質ガスから反応ガスへ移動する熱量をＱとすれば
Ｑ＝ＫＡΔＴ ・・・・・・ （１）
Ｋ：熱通過率
Ａ：伝熱面積
ΔＴ：温度差 で表わされる。Since the reforming reaction is an endothermic reaction, the CO conversion catalyst layer 1
Endotherm is absorbed from the reformed gas flowing through the heating layer 5 and the combustion gas flowing through the heating layer 16.Next, the reformed gas that has undergone the reforming reaction is supplied to the CO conversion catalyst layer 15, where it gradually undergoes a CO conversion reaction. The reformed gas is extracted from the reformed gas outlet 8. The temperature of the reformed gas is always higher than that of the reaction gas during the reforming reaction, and the CO conversion reaction is an exothermic reaction.
More heat can be supplied to the reforming catalyst layer 14. At this time, if the amount of heat transferred from the reformed gas to the reaction gas is Q, then Q=KAΔT... (1)
K: Heat transfer rate A: Heat transfer area ΔT: Temperature difference.
ここでＡを一定と考えれば、ＣＯ転化反応により改質ガ
ス温度が高くなるのでΔＴ、Ｋが共に大きくなり、従っ
てＱが大きくなる。従来のＣＯ転化触媒の設けられてい
ない改質装置に対する本発明の燃料改質装置のＱは約１
．２倍となり、燃焼量を減らすことが出来、高効率化を
達成出来る。また、Ｑを一定と考えればＡを小さくする
ことが出来る。従来技術の反応管長さに対する本発明の
反応管長さは約０．９倍となり改質装置の小型化が達成
される。従って、小型・コンパクト化に合つた改質装置
の選択が可能となる。Here, assuming that A is constant, the temperature of the reformed gas increases due to the CO conversion reaction, so both ΔT and K become large, and therefore Q becomes large. The Q of the fuel reformer of the present invention compared to a conventional reformer without a CO conversion catalyst is about 1.
．． The amount of fuel is doubled, reducing the amount of combustion and achieving high efficiency. Furthermore, if Q is considered constant, A can be made small. The length of the reaction tube of the present invention is about 0.9 times that of the conventional technology, and the size of the reformer can be reduced. Therefore, it is possible to select a reformer suitable for downsizing and compactness.
一方、燃料は燃料人口９を通って前記燃焼装置１２に供
給され、空気入口１０を通って供給された空気により燃
焼する。燃焼ガスは前記加熱層１６を通り、前記改質触
媒層１４に熱を供給して燃焼ガス出口１１より導き出さ
れる。Meanwhile, fuel is supplied to the combustion device 12 through the fuel port 9 and is combusted by air supplied through the air inlet 10. The combustion gas passes through the heating layer 16, supplies heat to the reforming catalyst layer 14, and is led out from the combustion gas outlet 11.
上記本実施例において、改質触媒としては、例えば、Ｎ
ｉ系のものが用いられる。また、ＣＯ転化触媒としては
、Ｆｅ−Ｃｒ系のものを用いることができる。In this embodiment, the reforming catalyst is, for example, N
i-series is used. Further, as the CO conversion catalyst, a Fe-Cr type catalyst can be used.
上記本実施例においては、二重管構造となっており、Ｃ
Ｏ転化触媒層の回りに改質触媒層が隣接して配置されて
いるために、熱効率がさらに向上する。なお、二重管の
内管と外管との間の隔壁は。In this embodiment, it has a double pipe structure, and C
Since the reforming catalyst layer is arranged adjacent to the O conversion catalyst layer, thermal efficiency is further improved. In addition, the partition wall between the inner tube and outer tube of the double tube.
波形、フィン状であっても良い。It may be wave-shaped or fin-shaped.
第２図には５第１図に示した本発明の実施例及び従来の
ｃｏ転化触媒が設けられていない改質装置の温度分布及
び反応率の分布を表すグラフを示す、比較の為、反応管
先端部の燃焼温度３０．原料入口温度２８及び反応平衡
温度２９を同一とした。FIG. 2 shows a graph showing the temperature distribution and reaction rate distribution of the example of the present invention shown in FIG. 1 and the conventional reformer without a co-conversion catalyst. Combustion temperature at the tip of the tube 30. The raw material inlet temperature 28 and the reaction equilibrium temperature 29 were made the same.
改質触媒層１４に入った原料は反応率２６，２７に示す
様急激に反応を始めるため１反応ガス温度２２．２３は
急激に温度低下を伴う、上記本発明の一実施例装置にお
ける反応ガス温度２２が従来装置の反応ガス温度２３に
較べて高いのは１本発明装置の燃焼ガス温度２０及び改
質ガス温度２４が従来装置の燃焼ガス温度２１及び改質
ガス温度２５に比較して高く、熱伝達が良いためである
。Since the raw material entering the reforming catalyst layer 14 starts to react rapidly as shown in reaction rates 26 and 27, 1 reaction gas temperature 22.23 is the reaction gas in the apparatus according to the embodiment of the present invention, which is accompanied by a sudden temperature drop. The reason why the temperature 22 is higher than the reaction gas temperature 23 of the conventional device is because the combustion gas temperature 20 and reformed gas temperature 24 of the device of the present invention are higher than the combustion gas temperature 21 and the reformed gas temperature 25 of the conventional device. , because of good heat transfer.
反応ガス温度２２．２３は徐々に上昇し、反応平衡温度
２９に達する。この場合、本発明装置の反応管長さは従
来装置の反応管、長さに対して１割短くても良い、改質
反応終了後の改質ガスは反応ガスに熱を供給するため、
徐々に温度降下する０本発明装置の改質ガス温度２４は
、ＣＯ転化反応による発熱のため従来装置の改質ガス温
度２５に較べ温度降下が少ない、燃焼ガス温度の温度降
下が体さいことも、ＣＯ転化反応における発熱を有効利
用していることを意味する。The reaction gas temperature 22.23 gradually increases and reaches the reaction equilibrium temperature 29. In this case, the length of the reaction tube of the apparatus of the present invention may be 10% shorter than that of the conventional apparatus, since the reformed gas supplies heat to the reaction gas after the reforming reaction is completed.
The temperature of the reformed gas 24 of the device of the present invention, which gradually decreases in temperature, is smaller than the reformed gas temperature 25 of the conventional device due to the heat generated by the CO conversion reaction, and the temperature drop of the combustion gas temperature may be small. , which means that the heat generated in the CO conversion reaction is effectively utilized.
本発明装置によれ−ば、全体的に温度レベルが高くなり
、改質反応が促進されることとなる。さらに、前記内管
３内側に前記ＣＯ転化触媒４を充填したことにより燃料
改質装置出口改質ガスのＣＯ濃度を下げることが出来、
ＣＯ転化装置（以下シフトコンバータと言う）内のＣＯ
転化触媒量の削減が可能となり、シフトコンバータの小
型化を達成出来るうえ、例えば、燃料電池発電システム
に利用された場合、システム全体の小型化も可能となる
。According to the apparatus of the present invention, the overall temperature level becomes high and the reforming reaction is promoted. Furthermore, by filling the inside of the inner pipe 3 with the CO conversion catalyst 4, it is possible to lower the CO concentration of the reformed gas at the exit of the fuel reformer,
CO in the CO conversion device (hereinafter referred to as shift converter)
This makes it possible to reduce the amount of conversion catalyst, making it possible to downsize the shift converter, and, for example, when used in a fuel cell power generation system, it also becomes possible to downsize the entire system.
第３図にＣＯ転化触媒４の耐熱温度が低い場合の本発明
の他の実施例の縦断面構成図を示す。FIG. 3 shows a vertical cross-sectional configuration diagram of another embodiment of the present invention in which the CO conversion catalyst 4 has a low allowable temperature limit.
原料ガス入ロアから供給された原料は、改質触媒層１４
に導かれ改質反応を行う、改質反応に要する熱量は加熱
層１６を流れる燃焼ガス及び内管３内側を流れる改質ガ
スによって与えられる。前記内管３内側の先端部には伝
熱粒子１３Ａが充填されており、前記伝熱粒子１３Ａの
上にはＣＯ転化触媒４が充填されている。前記充填粒子
１３Ａの充填層高さはｃｏ転化触媒４の耐熱温度により
決まる。すなわち、ＣＯ転化触媒の耐熱温度が低い場合
は、伝熱粒子の充填層高さを大きくする。The raw material supplied from the raw material gas input lower is transferred to the reforming catalyst layer 14.
The amount of heat required for the reforming reaction is given by the combustion gas flowing through the heating layer 16 and the reformed gas flowing inside the inner tube 3. The inner tip of the inner tube 3 is filled with heat transfer particles 13A, and the CO conversion catalyst 4 is filled on top of the heat transfer particles 13A. The height of the packed bed of the packed particles 13A is determined by the allowable temperature limit of the co conversion catalyst 4. That is, when the allowable temperature limit of the CO conversion catalyst is low, the height of the packed bed of heat transfer particles is increased.
現在のところ、Ｇｏ転化触媒の耐熱温度は、はぼ６００
℃であり、伝熱粒子１３Ａが充填された部分は、温度が
高い（約８００℃）ため、Ｇｏ−＋Ｃｏ２の反応が進み
にくい、このため、ＣＯ転化触媒ではなく伝熱粒子１３
Ａが充填されている。改質反応の終了した改質ガスは、
前記内管３内側の伝熱粒子層１３Ａを通りＣＯ転化触媒
４で反応し、改質ガス出口８より導き出される。前記第
１の実施例と比較して、ＣＯ転化触媒量は少ないが、反
応量は触媒層出口温度により決められるので、本実施例
のＣＯ転化触媒層１５での発熱量も先の実施例と本質的
には同じとなる。At present, the heat resistance temperature of the Go conversion catalyst is approximately 600℃.
℃, and the temperature of the part filled with the heat transfer particles 13A is high (approximately 800℃), so the reaction of Go-+Co2 does not proceed easily.
A is filled. The reformed gas after the reforming reaction is
It passes through the heat transfer particle layer 13A inside the inner tube 3, reacts with the CO conversion catalyst 4, and is led out from the reformed gas outlet 8. Although the amount of CO conversion catalyst is smaller than that of the first embodiment, since the amount of reaction is determined by the temperature at the outlet of the catalyst layer, the amount of heat generated in the CO conversion catalyst layer 15 of this embodiment is also similar to that of the previous embodiment. They are essentially the same.
本発明の他の実施例の斜視図を第４図に示す。A perspective view of another embodiment of the invention is shown in FIG.
さらに、第５図に本実施例装置の縦断面図、第６図にそ
の横断面図を示す。Furthermore, FIG. 5 shows a longitudinal cross-sectional view of the apparatus of this embodiment, and FIG. 6 shows a cross-sectional view thereof.
外筒３１と内筒３２との間に偶数個のらせん板１８を配
置し、前記外筒３１、前記内筒３２及び前記らせん板１
８により形成されるらせん状の空間部分に改質触媒２を
一空間おきに充填し、改質触媒層１４を形成する。前記
改質触媒層１４の両側には、高温ガス流路となる加熱層
１６を隣接しており、この加熱層１６には高温ガスから
前記改質触媒層１４への伝熱促進を図るため伝熱粒子１
３が充填されている。また、熱源として必要な熱量を発
生させるため、前記加熱層１６の燃料・空気入口に燃焼
触媒１９を充填している。前記改質触媒２）前記燃焼触
媒１９及び前記伝熱粒子１３は、セラミック製のハニカ
ム状支持板により固定している。前記内筒３２の内側に
はｃｏ転化触媒が充填され、ＣＯ転化触媒層１５と成る
。原料は原料人ロアを通って前記改質触媒層１４に供給
される。前記改質触媒層１４に入った原料は、前記らせ
ん板１８を介して前記加熱層１６を通過する高温ガス及
び前記内筒３２を介して改質ガスから熱を受け、改質反
応の進行と共に水素富化な改質ガスとなる。生成した改
質ガスは前記内筒３２に集められＣＯ転化触媒層１５に
供給され、反応ガスに熱を奪われることによりＣＯ転化
反応が促進され、ＣＯの少ない改質ガスとなり改質ガス
出口８より取り出される。一方、反応ガスの加熱源とな
る高温ガスは、前記加熱層１６の燃料・空気入口に充填
した前記燃焼触媒１９で燃料を燃やすことにより得られ
る０発生した高温燃焼ガスは、前記加熱層１６を通るこ
とにより前記らせん板１８を介して前記改質触媒層１４
に熱を与える。これは、前記伝熱粒子１３の存在により
、対流、伝導・輻射の伝熱係態が有効に作用して行なわ
れる。前記改質触媒層１４を加熱した高温ガスは温度で
降下し、排ガスとして、排気管より排気される０本実施
例ではｃｏ転化反応による発熱を有効に利用出来るので
燃料の削減が可能となり、構造上デッドスペースが無く
なり、大幅な小型化が達成出来。An even number of spiral plates 18 are arranged between the outer cylinder 31 and the inner cylinder 32, and the outer cylinder 31, the inner cylinder 32 and the spiral plate 1
The reforming catalyst 2 is filled in every other space in the spiral space formed by the reforming catalyst 8 to form the reforming catalyst layer 14. Adjacent to both sides of the reforming catalyst layer 14 are heating layers 16 that serve as high-temperature gas flow paths. thermal particle 1
3 is filled. Further, in order to generate the necessary amount of heat as a heat source, a combustion catalyst 19 is filled in the fuel/air inlet of the heating layer 16. The reforming catalyst 2) The combustion catalyst 19 and the heat transfer particles 13 are fixed by a ceramic honeycomb support plate. The inside of the inner cylinder 32 is filled with a CO conversion catalyst to form the CO conversion catalyst layer 15. The raw material is supplied to the reforming catalyst bed 14 through the raw material lower. The raw material that has entered the reforming catalyst layer 14 receives heat from the high-temperature gas passing through the heating layer 16 via the spiral plate 18 and from the reformed gas via the inner cylinder 32, and as the reforming reaction progresses. The result is hydrogen-enriched reformed gas. The generated reformed gas is collected in the inner cylinder 32 and supplied to the CO conversion catalyst layer 15, where heat is taken away by the reaction gas to promote the CO conversion reaction, resulting in a reformed gas with less CO and a reformed gas outlet 8. taken out from On the other hand, the high-temperature gas that serves as a heating source for the reaction gas is obtained by burning fuel with the combustion catalyst 19 filled in the fuel/air inlet of the heating layer 16.The generated high-temperature combustion gas is By passing through the helical plate 18, the reforming catalyst layer 14
give heat to. This is accomplished by the effective effects of convection, conduction, and radiation heat transfer due to the presence of the heat transfer particles 13. The high-temperature gas that heated the reforming catalyst layer 14 is lowered in temperature and is exhausted from the exhaust pipe as exhaust gas.In this embodiment, the heat generated by the CO conversion reaction can be effectively used, making it possible to reduce fuel consumption. There is no dead space on the top, making it possible to achieve significant downsizing.
体積は約１７４とすることが可能となる。また。The volume can be approximately 174. Also.
改質触媒は、らせん状に保持されるため、触媒自体の重
量による破壊を防止できる。Since the reforming catalyst is held in a spiral shape, it can be prevented from being destroyed by the weight of the catalyst itself.
以上説明したように本発明によれば、改質触媒が充填さ
れた第１のガス流通路と、ＣＯ転化触媒が充填された第
２のガス流通路とが隣接されて設けられているため、温
度差による伝熱に加えて。As explained above, according to the present invention, since the first gas flow passage filled with a reforming catalyst and the second gas flow passage filled with a CO conversion catalyst are provided adjacently, In addition to heat transfer due to temperature differences.
ＣＯ→ＣＯ□転化反応による発熱を利用して改質反応を
行うことができる。したがって、熱伝達の向上によりそ
の分装置の小型・コンパクト化が達成でき、かつ、熱効
率が向上し燃料の消費量を低減できる。The reforming reaction can be carried out using the heat generated by the CO→CO□ conversion reaction. Therefore, by improving heat transfer, the device can be made smaller and more compact, and the thermal efficiency can be improved and fuel consumption can be reduced.
第１図は本発明の実施装置の縦断面図構成図、第２図は
、改質装置の温度分布及び反応率の比較のグラフ、第３
図または第４図は本発明の他の実施例の構成を示す一部
透視斜視図、第５図は第４図の実施例装置の縦断面構成
図、第６図は第４図の実施例装置の横断面構成図である
。
１・・・外管、２・・・改質触媒、３・・・内管、４・
・・ＣＯ転化触媒、５・・・胴、６・・・原料入口、８
・・・改質ガス、９・・・燃料入口、１０・・・空気入
口、１１・・・燃焼ガス出口、１２・・・燃焼装置、１
３・・・伝熱粒子、１４・・・改質触媒層。
１５・・・Ｇｏ転化触媒層、１６・・・加熱層、１７・
・・燃料・空気入口、１８・・・らせん板、１９・・・
燃焼触媒、
２０・・・本発明による燃焼ガス温度。
２１・・・従来技術による燃焼ガス温度、２２・・・本
発明による反応ガス温度。
２３・・・従来技術による反応ガス温度、２４・・・本
発明による改質ガス温度、２５・・・従来技術による改
質ガス温度、２６・・・本発明による反応率、
２７・・・従来技術による反応率、
２８・・・原料入口温度、２９゛・・・反応平衡温度。
３０・・・燃焼温度、３１・・・外筒、３２・・・内筒
。FIG. 1 is a vertical cross-sectional view and configuration diagram of the apparatus for implementing the present invention, FIG. 2 is a graph comparing the temperature distribution and reaction rate of the reformer, and FIG.
4 is a partially transparent perspective view showing the configuration of another embodiment of the present invention, FIG. 5 is a vertical cross-sectional configuration diagram of the embodiment device of FIG. 4, and FIG. 6 is an embodiment of the embodiment of FIG. 4. FIG. 2 is a cross-sectional configuration diagram of the device. 1...Outer tube, 2...Reforming catalyst, 3...Inner tube, 4...
... CO conversion catalyst, 5 ... cylinder, 6 ... raw material inlet, 8
... Reformed gas, 9... Fuel inlet, 10... Air inlet, 11... Combustion gas outlet, 12... Combustion device, 1
3... Heat transfer particles, 14... Reforming catalyst layer. 15... Go conversion catalyst layer, 16... Heating layer, 17.
...Fuel/air inlet, 18...Spiral plate, 19...
Combustion catalyst, 20... Combustion gas temperature according to the present invention. 21... Combustion gas temperature according to the prior art, 22... Reaction gas temperature according to the present invention. 23... Reaction gas temperature according to the prior art, 24... Reformed gas temperature according to the present invention, 25... Reformed gas temperature according to the prior art, 26... Reaction rate according to the present invention, 27... Conventional Reaction rate by technology, 28... Raw material inlet temperature, 29゛... Reaction equilibrium temperature. 30... Combustion temperature, 31... Outer cylinder, 32... Inner cylinder.
Claims (4)
該通路に原料ガスを供給する原料ガス供給手段と、前記
第１のガス流通路内の原料ガスに熱量を付与する伝熱手
段と、前記第１のガス流通路内の原料ガスが改質された
改質ガスを取り出す取り出し手段とを備えてなる燃料改
質装置において、前記第１のガス流通路に隣接されて設
けられ、内部にＣＯ転化触媒が充填されてなる第２のガ
ス流通路と、前記第１のガス流通路から出たガスが当該
第２のガス流通路に導くための改質ガス導入部とが設け
られていることを特徴とする燃料改質装置。(1) a first gas flow path filled with a reforming catalyst;
a raw material gas supply means for supplying raw material gas to the passage; a heat transfer means for imparting heat to the raw material gas in the first gas flow passage; and a raw material gas in the first gas flow passage to be reformed. a second gas flow path provided adjacent to the first gas flow path and filled with a CO conversion catalyst; , and a reformed gas introduction section for guiding gas discharged from the first gas flow path to the second gas flow path.
流通路と第２のガス流通路とは、二重管構造とから構成
され、当該二重管の内部にＣＯ転化触媒が充填されてな
ることを特徴とする燃料改質装置。(2) In claim 1, the first gas flow path and the second gas flow path are constructed of a double pipe structure, and the inside of the double pipe is filled with a CO conversion catalyst. A fuel reformer characterized by:
記第２のガス流通路の前記改質ガス導入部側先端部に、
伝熱粒子が充填されてなることを特徴とする燃料改質装
置。(3) In claim 1 or 2, at the tip of the second gas flow path on the reformed gas introduction section side,
A fuel reformer characterized by being filled with heat transfer particles.
項において、前記ガス流通路がらせん状に形成されてな
ることを特徴とする燃料改質装置。(4) Any one of claims 1 to 3
2. The fuel reformer according to item 1, wherein the gas flow passage is formed in a spiral shape.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63004533A JP2646101B2 (en) | 1988-01-12 | 1988-01-12 | Fuel reformer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63004533A JP2646101B2 (en) | 1988-01-12 | 1988-01-12 | Fuel reformer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01183401A true JPH01183401A (en) | 1989-07-21 |
| JP2646101B2 JP2646101B2 (en) | 1997-08-25 |
Family
ID=11586684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63004533A Expired - Lifetime JP2646101B2 (en) | 1988-01-12 | 1988-01-12 | Fuel reformer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2646101B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998000361A1 (en) * | 1996-06-28 | 1998-01-08 | Matsushita Electric Works, Ltd. | Modification apparatus |
| EP1020400A1 (en) * | 1999-01-15 | 2000-07-19 | DBB Fuel Cell Engines Gesellschaft mit beschränkter Haftung | Device for the combination of two heterogeneous catalytic reactions |
| JP2002249302A (en) * | 2001-02-16 | 2002-09-06 | Nippon Chem Plant Consultant:Kk | Method and apparatus for reforming by internal heating- type oxidation |
| JP2009274919A (en) * | 2008-05-15 | 2009-11-26 | Univ Of Yamanashi | External heat type hydrogen production apparatus and fuel cell power system using the same |
| JP2010235346A (en) * | 2009-03-30 | 2010-10-21 | Japan Energy Corp | Self-heated oxidation reforming apparatus and fuel cell system |
| JP2010235348A (en) * | 2009-03-30 | 2010-10-21 | Japan Energy Corp | Self-heated oxidation reforming apparatus and fuel cell system |
| JP2011201729A (en) * | 2010-03-25 | 2011-10-13 | Jx Nippon Oil & Energy Corp | Reforming device and fuel cell system |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6227489A (en) * | 1985-07-26 | 1987-02-05 | Chiyoda Chem Eng & Constr Co Ltd | Steam reforming device |
-
1988
- 1988-01-12 JP JP63004533A patent/JP2646101B2/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6227489A (en) * | 1985-07-26 | 1987-02-05 | Chiyoda Chem Eng & Constr Co Ltd | Steam reforming device |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998000361A1 (en) * | 1996-06-28 | 1998-01-08 | Matsushita Electric Works, Ltd. | Modification apparatus |
| US6413479B1 (en) | 1996-06-28 | 2002-07-02 | Matsushita Electric Works, Ltd. | Reforming apparatus for making a co-reduced reformed gas |
| USRE39675E1 (en) | 1996-06-28 | 2007-06-05 | Matsushita Electric Works, Ltd. | Reforming apparatus for making a co-reduced reformed gas |
| EP1020400A1 (en) * | 1999-01-15 | 2000-07-19 | DBB Fuel Cell Engines Gesellschaft mit beschränkter Haftung | Device for the combination of two heterogeneous catalytic reactions |
| JP2002249302A (en) * | 2001-02-16 | 2002-09-06 | Nippon Chem Plant Consultant:Kk | Method and apparatus for reforming by internal heating- type oxidation |
| JP2009274919A (en) * | 2008-05-15 | 2009-11-26 | Univ Of Yamanashi | External heat type hydrogen production apparatus and fuel cell power system using the same |
| JP2010235346A (en) * | 2009-03-30 | 2010-10-21 | Japan Energy Corp | Self-heated oxidation reforming apparatus and fuel cell system |
| JP2010235348A (en) * | 2009-03-30 | 2010-10-21 | Japan Energy Corp | Self-heated oxidation reforming apparatus and fuel cell system |
| JP2011201729A (en) * | 2010-03-25 | 2011-10-13 | Jx Nippon Oil & Energy Corp | Reforming device and fuel cell system |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2646101B2 (en) | 1997-08-25 |
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