JPH0891802A - Modifying device of methanol - Google Patents
Modifying device of methanolInfo
- Publication number
- JPH0891802A JPH0891802A JP6257673A JP25767394A JPH0891802A JP H0891802 A JPH0891802 A JP H0891802A JP 6257673 A JP6257673 A JP 6257673A JP 25767394 A JP25767394 A JP 25767394A JP H0891802 A JPH0891802 A JP H0891802A
- Authority
- JP
- Japan
- Prior art keywords
- methanol
- porous body
- reaction
- reaction vessel
- catalyst layer
- 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.)
- Pending
Links
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 242
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- 239000003054 catalyst Substances 0.000 claims abstract description 55
- 238000006722 reduction reaction Methods 0.000 claims abstract description 18
- 239000012530 fluid Substances 0.000 claims abstract description 12
- 238000002407 reforming Methods 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 abstract description 6
- 230000000149 penetrating effect Effects 0.000 abstract description 2
- 239000010410 layer Substances 0.000 description 37
- 239000007789 gas Substances 0.000 description 23
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 229910052763 palladium Inorganic materials 0.000 description 3
- 229910052697 platinum Inorganic materials 0.000 description 3
- 229910052709 silver Inorganic materials 0.000 description 3
- 239000004332 silver Substances 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 238000005219 brazing Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000006262 metallic foam Substances 0.000 description 2
- 125000001570 methylene group Chemical group [H]C([H])([*:1])[*:2] 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 239000011247 coating layer Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 239000011888 foil Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Landscapes
- Hydrogen, Water And Hydrids (AREA)
- Catalysts (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、一般にはメタノ−ルを
還元反応により一酸化炭素および水素に変えるための改
質装置に関し、特にデイ−ゼルエンジンの燃料として使
用されるメタノ−ルの改質装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates generally to a reformer for converting methanol into carbon monoxide and hydrogen by a reduction reaction, and more particularly to a reformer of methanol used as a fuel for diesel engines. Regarding quality equipment.
【０００２】[0002]
【従来の技術】メタノ−ルは窒素酸化物等の有毒な排気
ガスを出さないクリ−ンな燃料としてデイ−ゼルエンジ
ン等への利用が研究されている。メタノ−ルをデイ−ゼ
ルエンジン用の燃料として使用する場合、（１）式で表
される還元反応によりメタノ−ル（ＣＨ3 ＯＨ）を一酸
化炭素（ＣＯ）および水素ガス（Ｈ2 ）に分解した後
に、エンジンの燃焼室に供給して燃焼させる。 ＣＨ3 ＯＨ ＝ ＣＯ ＋ ２Ｈ2 （１） この還元反応を進行させるためには、例えば白金または
パラジウムのような活性金属を触媒として用いる必要が
あり、さらにこの触媒による還元反応を効率的に進行さ
せるためには、触媒自体を約４００℃以上の高温に維持
することが望ましい。2. Description of the Related Art The use of methanol as a clean fuel that does not emit toxic exhaust gas such as nitrogen oxides has been studied for use in diesel engines. When methanol is used as a fuel for a diesel engine, methanol (CH 3 OH) is converted into carbon monoxide (CO) and hydrogen gas (H 2 ) by a reduction reaction represented by the formula (1). After the decomposition, it is supplied to the combustion chamber of the engine for combustion. CH 3 OH = CO + 2H 2 (1) In order to promote this reduction reaction, it is necessary to use an active metal such as platinum or palladium as a catalyst, and further the reduction reaction by this catalyst is allowed to proceed efficiently. Therefore, it is desirable to maintain the catalyst itself at a high temperature of about 400 ° C. or higher.
【０００３】触媒自体の加熱は、何らかの熱源に直接的
または間接的に触媒を接触させて行なえばよいが、この
加熱を効率的に行なうためには触媒の熱源への接触面積
をできるだけ大きくしてやる必要がある。また、同時に
触媒と反応物質であるメタノ−ルとの接触面積も大きく
なければ還元反応が充分には進行しない。従って、メタ
ノ−ルの改質、すなわち（１）式で表される還元反応を
効率的に進行させるためには、使用される触媒が熱源お
よびメタノ−ルの両者に充分な接触面積を持っているこ
とが必要である。The heating of the catalyst itself may be carried out by directly or indirectly bringing the catalyst into contact with some heat source, but in order to perform this heating efficiently, it is necessary to make the contact area of the catalyst with the heat source as large as possible. There is. At the same time, the reduction reaction does not proceed sufficiently unless the contact area between the catalyst and methanol as a reactant is large. Therefore, in order to efficiently progress the reforming of methanol, that is, the reduction reaction represented by the formula (1), the catalyst used has a sufficient contact area with both the heat source and the methanol. Need to be present.
【０００４】[0004]
【発明が解決しようとする課題】従来使用されている触
媒は、反応物質であるメタノ−ルとの接触面積を大きく
するために比表面積が大きい球状またはペレット状の形
状をしたものが多い。しかしながら、この場合、触媒と
熱源との接触面積が小さく効率よく触媒を加熱すること
ができないという欠点があった。また、球状またはペレ
ット状の場合、メタノ−ルの流れに対して圧力損失が大
きいという欠点もあった。Most of the conventionally used catalysts have a spherical or pellet-like shape with a large specific surface area in order to increase the contact area with the reactant methanol. However, in this case, there is a drawback that the contact area between the catalyst and the heat source is small and the catalyst cannot be efficiently heated. Further, in the case of a spherical shape or a pellet shape, there is a drawback that the pressure loss is large with respect to the flow of methanol.
【０００５】この欠点を解決するために、特開昭６３−
７８４３号公報には、メタノ−ルの改質用触媒層とし
て、アルミナにチタニアをコ−テイングしたものを焼成
した担体に白金またはパラジウムのような活性金属を担
持させたものが開示されている。この場合、触媒層がア
ルミナ上に一様に形成されているので、アルミナを加熱
することにより触媒層を充分に加熱することができる。
しかしながら、この触媒層を用いた場合においても、触
媒層表面からの距離が離れるにつれてメタノ−ルの還元
反応が進行しにくくなるので、ある程度空間的に広がっ
た領域に渡るメタノ−ル流に対して還元反応を進行させ
るためには、触媒層が設けられたアルミナ基体を一定間
隔ごとに空間的に多数配置しなければならず、メタノ−
ルの改質装置としては構造が複雑かつ大がかりなものに
ならざるを得ないという欠点がある。In order to solve this drawback, Japanese Patent Laid-Open No. 63-
Japanese Patent No. 7843 discloses a catalyst layer for reforming methanol, in which an active metal such as platinum or palladium is carried on a carrier obtained by firing a product obtained by coating titania on alumina. In this case, since the catalyst layer is uniformly formed on the alumina, the catalyst layer can be sufficiently heated by heating the alumina.
However, even when this catalyst layer is used, the reduction reaction of methanol becomes difficult to proceed as the distance from the surface of the catalyst layer increases, so that the methanol flow over a spatially spread region to some extent In order to proceed the reduction reaction, a large number of alumina substrates provided with a catalyst layer must be spatially arranged at regular intervals.
However, there is a drawback in that the structure of the reformer for hydrogen is complicated and large-scale.
【０００６】本発明は、上記した欠点を解決するために
なされたもので、その目的とするところは、メタノ−ル
の改質に使用される触媒を効率的に所定の高温に維持す
ることができ、かつメタノ−ルと触媒との接触面積が大
きく、またメタノ−ルの流れに対して圧力損失の小さく
できる、反応効率の高いメタノ−ルの改質装置を提供す
ることである。The present invention has been made to solve the above-mentioned drawbacks, and an object thereof is to efficiently maintain a catalyst used for reforming methanol at a predetermined high temperature. It is an object of the present invention to provide a reformer for methanol which has a high reaction efficiency and which has a large contact area between the methanol and the catalyst and can reduce the pressure loss with respect to the flow of the methanol.
【０００７】[0007]
【課題を解決するための手段】前記目的を達成するため
に、本発明によれば、高温流体が流れる流路を形成する
第１の手段と、前記第１の手段を取り囲んで配設され
た、メタノ−ルが流れる流路を形成する第２の手段と、
を有するメタノ−ルの改質装置において、前記第２の手
段が前記第１の手段に接合された多孔質体を含み、前記
多孔質体の開口部表面にメタノ−ルの化学反応を進行さ
せるために必要な触媒層を設け、前記高温流体から前記
触媒層への熱伝達率を高めて前記多孔質体中を流れるメ
タノ−ルの化学反応効率を向上させるようにしたことを
特徴とするメタノ−ルの改質装置が提供される。In order to achieve the above object, according to the present invention, there are provided a first means for forming a flow path through which a high temperature fluid flows, and a first means arranged to surround the first means. , Second means for forming a flow path through which the methanol flows,
In the reforming apparatus of methanol, the second means includes a porous body joined to the first means, and a chemical reaction of methanol proceeds on the surface of the opening of the porous body. In order to improve the chemical reaction efficiency of methanol flowing through the porous body by providing a catalyst layer necessary for increasing the heat transfer coefficient from the high temperature fluid to the catalyst layer. A reformer of the reactor is provided.
【０００８】また、本発明によれば、メタノ−ルの供給
口と、メタノ−ルの反応後に発生するガスを排出するた
めの排出口とを有する反応容器と、前記反応容器内に収
められたメタノ−ルの反応槽と、前記反応容器を貫通し
て配設された高温ガスが流れる１つまたは２つ以上の管
と、を有するメタノ−ルの改質装置において、前記反応
槽が前記反応容器内壁および前記管の外壁に接合された
多孔質体からなり、前記多孔質体の開口部表面にメタノ
−ルの還元反応を進行させるために必要な触媒層を設
け、前記高温ガスから前記触媒層への熱伝達率を高めて
前記多孔質体中を流れるメタノ−ルの還元反応効率を向
上させるようにしたことを特徴とするメタノ−ルの改質
装置が提供される。Further, according to the present invention, a reaction container having a supply port for methanol and a discharge port for discharging a gas generated after the reaction of methanol, and the reaction container are housed in the reaction container. In a methanol reforming device having a methanol reaction tank and one or more pipes through which the high temperature gas flows, which is arranged so as to penetrate through the reaction container, the reaction tank is used for the reaction. It is composed of a porous body bonded to the inner wall of the container and the outer wall of the tube, and a catalyst layer necessary for advancing the reduction reaction of methanol is provided on the surface of the opening of the porous body, and the catalyst is formed from the high temperature gas. A reforming device for methanol is provided, which is characterized in that the heat transfer coefficient to the layer is increased to improve the reduction reaction efficiency of the methanol flowing in the porous body.
【０００９】さらに、本発明によれば、デイ−ゼルエン
ジンからの排気ガスの入り口と、前記排気ガスの排出口
と、メタノ−ルの供給口と、メタノ−ルの反応後に発生
するガスを排出するための排出口とを有する反応容器
と、前記反応容器内に収められたメタノ−ルの反応槽
と、前記反応槽を貫通して配設された前記排気ガスが流
れる１つまたは２つ以上の管と、を有するデイ−ゼルエ
ンジンの排気管に接合されたデイ−ゼルエンジン用メタ
ノ−ルの改質装置において、前記反応槽が前記反応容器
内壁および前記管の外壁に接合された、前記管を構成す
る材質の熱膨脹係数とほぼ等しい熱膨脹係数を有する多
孔質体からなり、前記多孔質体の開口部表面に触媒層が
設けられ、前記排気ガスから前記触媒層への熱伝達率を
高めて前記多孔質体中を流れるメタノ−ルの還元反応効
率を向上させるようにしたことを特徴とするデイ−ゼル
エンジン用メタノ−ルの改質装置が提供される。Further, according to the present invention, the exhaust gas inlet from the diesel engine, the exhaust gas exhaust port, the methanol supply port, and the gas generated after the reaction of the methanol are exhausted. A reaction vessel having a discharge port for discharging the reaction gas, a reaction vessel for methanol contained in the reaction vessel, and one or more of the exhaust gas flowing through the reaction vessel through which the exhaust gas flows. A reformer of a methanol for a diesel engine joined to an exhaust pipe of a diesel engine, the reaction tank being joined to an inner wall of the reaction vessel and an outer wall of the pipe. It is made of a porous body having a thermal expansion coefficient substantially equal to the thermal expansion coefficient of the material forming the tube, and a catalyst layer is provided on the surface of the opening of the porous body to enhance the heat transfer coefficient from the exhaust gas to the catalyst layer. In the porous body For diesel engines methanol - - Le reformer is provided Day characterized in that so as to improve the reduction reaction efficiency of Le - methanol flow.
【００１０】[0010]
【作用】本発明のメタノ−ルの改質装置においては、メ
タノ−ルの化学反応が起こる反応槽である多孔質体が熱
源である高温流体が流れる手段に直接接合されており、
さらに多孔質体開口部表面に触媒層が設けられている。
したがって、触媒層の熱源への接触面積が大きいので高
温流体から触媒層への熱伝達が効率よく行われ、触媒層
全体が高温に維持されやすく、かつ多孔質体の開口部を
流れるメタノ−ルと触媒層との接触面積が大きいので、
メタノ−ルの還元反応が効率的に行なわれる。In the methanol reforming apparatus of the present invention, the porous body, which is the reaction tank in which the chemical reaction of methanol occurs, is directly joined to the means through which the high-temperature fluid, which is the heat source, flows.
Further, a catalyst layer is provided on the surface of the opening of the porous body.
Therefore, since the contact area of the catalyst layer with the heat source is large, heat is efficiently transferred from the high temperature fluid to the catalyst layer, the entire catalyst layer is easily maintained at high temperature, and the methanol flowing through the opening of the porous body is Since the contact area between the and the catalyst layer is large,
The reduction reaction of methanol is efficiently performed.
【００１１】また、本発明のメタノ−ルの改質装置は、
反応槽を構成する多孔質体が高温流体が流れる管の材質
の熱膨脹係数とほぼ等しい熱膨脹係数を有するので、高
温下においても管と多孔質体との接合状態は安定してい
る。The methanol reforming apparatus of the present invention is
Since the porous body constituting the reaction tank has a coefficient of thermal expansion substantially equal to that of the material of the tube through which the high-temperature fluid flows, the bonded state of the tube and the porous body is stable even at high temperature.
【００１２】[0012]
【実施例】次に、本発明の実施例について図面を参照し
ながら説明する。図１は、本発明の一実施例のメタノ−
ルの改質装置の断面図である。同図の実施例は、デイ−
ゼルエンジンの排気管に接合されたデイ−ゼルエンジン
用メタノ−ルの改質装置１００を示したものである。本
実施例のメタノ−ルの改質装置１００において、円筒型
の反応容器１０の上部および下部にはフランジ１２、１
４が設けられている。そして、このフランジ部分におい
てメタノ−ルの改質装置１００と排気管２００、３００
とがボルトおよびナット１６、１７、１８、１９によっ
て接合されている。２０１、３０１は、排気管２００、
３００のフランジを示している。また、反応容器１０は
排気管２００、３００と同じＳＵＳで作られている。Embodiments of the present invention will now be described with reference to the drawings. FIG. 1 shows a methano of an embodiment of the present invention.
FIG. 3 is a cross-sectional view of a reforming device for a le. The embodiment shown in FIG.
1 shows a reformer 100 of a diesel engine methanol joined to an exhaust pipe of a diesel engine. In the methanol reforming apparatus 100 of this embodiment, flanges 12 and 1 are provided on the upper and lower portions of the cylindrical reaction vessel 10.
4 are provided. Then, in this flange portion, the reforming device 100 for the methanol and the exhaust pipes 200, 300
And are joined by bolts and nuts 16, 17, 18, 19. 201 and 301 are exhaust pipes 200,
A flange of 300 is shown. The reaction container 10 is made of the same SUS as the exhaust pipes 200 and 300.
【００１３】反応容器１０内には、反応槽として、反応
容器内壁と接合された円筒型の多孔質体２０が収められ
ている。多孔質体２０と反応容器１０の上部フランジ１
２との間には、スペ−スである気化層３０が設けられて
いる。そして、反応容器１０の気化層３０の外壁にあた
る部分にメタノ−ルの供給口４０が設けられている。ま
た、排気ガスが流れる複数の管５０が多孔質体２０を含
む反応容器１０を貫通して設けられており、各々の管の
外壁は多孔質体２０と接合されている。さらに、反応容
器１０の下部には、メタノ−ルの還元反応によって発生
する水素及び一酸化炭素ガスを排出するための排出口４
２が設けられている。A cylindrical porous body 20 joined to the inner wall of the reaction container is contained in the reaction container 10 as a reaction tank. Porous body 20 and upper flange 1 of reaction vessel 10
A vaporization layer 30 as a space is provided between the two. Further, a methanol supply port 40 is provided at a portion corresponding to the outer wall of the vaporization layer 30 of the reaction container 10. Further, a plurality of tubes 50 through which exhaust gas flows are provided so as to penetrate the reaction container 10 including the porous body 20, and the outer wall of each tube is joined to the porous body 20. Further, at the lower part of the reaction vessel 10, an exhaust port 4 for exhausting hydrogen and carbon monoxide gas generated by the reduction reaction of methanol.
2 are provided.
【００１４】排気管２００から入ってくる４００℃以上
の高温の排気ガスが、反応容器１０を貫通して設けられ
た複数の管５０内を流れて排気管３００へ排出される。
この高温の排気ガスが複数の管５０内を流れる過程にお
いて、排気ガスの熱が管外壁に接合された多孔質体２０
へ熱伝達される。そして、詳細が後述される多孔質体２
０の開口部表面に設けられた触媒層が４００℃程度の高
温に維持される。供給口４０から供給された液状のメタ
ノ−ルは、多孔質体２０がないスペ−スである気化層３
０で、高温の排気ガスが流れる管５０からの熱によって
気化された後、ガス状となって高温に維持された触媒層
が含れている多孔質体２０中を通過していく。この通過
の過程において、メタノ−ルは（１）式で表される還元
反応により水素及び一酸化炭素に分解されて排出口３２
から排出される。Exhaust gas having a high temperature of 400 ° C. or higher that enters from the exhaust pipe 200 flows through a plurality of pipes 50 penetrating the reaction vessel 10 and is discharged to the exhaust pipe 300.
In the process in which this high-temperature exhaust gas flows through the plurality of pipes 50, the heat of the exhaust gas is bonded to the outer wall of the pipe 20.
Heat is transferred to. And the porous body 2 whose details will be described later
The catalyst layer provided on the surface of the opening of No. 0 is maintained at a high temperature of about 400 ° C. The liquid methanol supplied from the supply port 40 is a space without the porous body 20 and is a vaporization layer 3
At 0, the high-temperature exhaust gas is vaporized by the heat from the pipe 50 and then passes through the porous body 20 containing the catalyst layer which has become gaseous and is maintained at a high temperature. In the course of this passage, methanol is decomposed into hydrogen and carbon monoxide by the reduction reaction represented by the formula (1), and the exhaust port 32
Emitted from.
【００１５】図２は、排気ガスを流すための複数の管５
０と一体となった円柱型の多孔質体２０の斜視図であ
る。複数の管５０は多孔質体１０を貫通して設けられて
いる。次に、この円筒型の多孔質体２０の製造方法につ
いて説明する。まず、円柱形に加工された金属多孔質体
からなるメタル・フォ−ムを用意し、これに管５０が通
る穴をあけ、管を通してメタル・フォ−ムと管を銀ろう
付け等により接合する。そして、メタル・フォ−ム全体
をアルミナＡｌ2 Ｏ3 が含まれた溶液中に浸す。その
際、管の中に溶液が入らないように予め管の入り口をふ
さいでおく。次に、溶液から取り出したメタル・フォ−
ムの乾燥および焼成を行なう。焼成は例えば７００℃で
行なう。この浸漬から焼成までの工程を、多孔質体の開
口部表面に１００ミクロン程度の厚さのアルミナＡｌ2
Ｏ3 のコ−テイング層が形成されるまで繰り返す。最後
に、このアルミナのコ−テイング層に白金またはパラジ
ウム等の触媒となる金属を担持させて触媒層を完成させ
る。以上の工程により、円柱型の多孔質体２０が出来上
がる。FIG. 2 shows a plurality of pipes 5 for flowing exhaust gas.
FIG. 3 is a perspective view of a cylindrical porous body 20 integrated with 0. The plurality of tubes 50 are provided so as to penetrate the porous body 10. Next, a method for manufacturing the cylindrical porous body 20 will be described. First, a metal foam made of a porous metal body processed into a cylindrical shape is prepared, a hole through which the pipe 50 passes is made in this, and the metal form and the pipe are joined by silver brazing or the like through the pipe. . Then, the entire metal foam is dipped in a solution containing alumina Al 2 O 3 . At that time, the inlet of the tube is previously closed so that the solution does not enter the tube. Next, the metal foil removed from the solution
Dry and bake the steam. The firing is performed at 700 ° C., for example. The process from the dipping to the firing is performed on the surface of the opening of the porous body by using alumina Al 2 having a thickness of about 100 μm.
O 3 co - repeated until Teingu layer is formed. Finally, a metal serving as a catalyst such as platinum or palladium is supported on the coating layer of alumina to complete the catalyst layer. Through the above steps, the cylindrical porous body 20 is completed.
【００１６】図３は、上記した製造工程により作られる
多孔質体２０の管５０との接合部近傍の様子を示した図
である。管の外壁と多孔質体とは銀ろう５２によって接
合され、多孔質体２０中には開口２２が一様に形成され
ている。この開口２２中を気化されたメタノ−ル・ガス
等が流れる。開口２２の平均的な大きさおよび開口２２
の数は、流れるガスの流量および圧力に応じて、必要な
ガスの流速および所定の圧力損失等が生ずるように決め
られる。多孔質体２０全体に対する開口２２の割合を表
す開口率をある程度大きく取った場合、流れるガスの圧
力損失が小さくできるので、球状またはペレット状の触
媒を用いた場合に比べて、メタノ−ルを供給するための
駆動圧力および駆動ポンプの容量を小さくすることが可
能である。また、管５０と多孔質体２０とは、同じ材質
たとえばＳＵＳでできている。従って、熱膨脹係数が等
しいので高温下においても熱膨脹係数の違いにより管５
０の外壁と多孔質体２０との接合状態が不安定になるこ
とはない。また熱伝達係数も等しいことから高温の排気
ガスからの熱が充分に多孔質２０体全体に熱伝達され
る。FIG. 3 is a view showing a state in the vicinity of a joint portion of the porous body 20 produced by the above-mentioned manufacturing process with the tube 50. The outer wall of the tube and the porous body are joined by silver brazing 52, and openings 22 are uniformly formed in the porous body 20. Vaporized methanol gas or the like flows through the opening 22. Average size of opening 22 and opening 22
Is determined so that a required gas flow rate, a predetermined pressure loss, and the like occur depending on the flow rate and pressure of the flowing gas. When the opening ratio, which represents the ratio of the openings 22 to the entire porous body 20, is set to be large to some extent, the pressure loss of the flowing gas can be reduced, so that the methanol is supplied as compared with the case where a spherical or pellet catalyst is used. It is possible to reduce the drive pressure and the capacity of the drive pump for controlling. The tube 50 and the porous body 20 are made of the same material, for example, SUS. Therefore, since the coefficients of thermal expansion are the same, even if the temperature of the tubes is high
The joint state between the outer wall of No. 0 and the porous body 20 does not become unstable. Further, since the heat transfer coefficients are the same, the heat from the hot exhaust gas is sufficiently transferred to the entire porous body 20.
【００１７】図４は、図３中の円Ａ部分の多孔質体２０
の表面に設けられた触媒層２４の様子を示した拡大図で
ある。触媒層２４は多孔質体２０の開口部表面に一様に
１００ミクロン程度の厚さで形成されている。このよう
に、触媒層２４は多孔質体２０の開口部表面に一様に形
成されているので、例えば排気ガス管表面にのみ形成さ
れた場合に比べて、実質上熱源に接触している表面積が
増加し効率よく触媒層を高温にすることができる。FIG. 4 shows the porous body 20 in the circle A portion in FIG.
FIG. 4 is an enlarged view showing a state of a catalyst layer 24 provided on the surface of the. The catalyst layer 24 is formed uniformly on the surface of the opening of the porous body 20 with a thickness of about 100 μm. As described above, since the catalyst layer 24 is uniformly formed on the surface of the opening of the porous body 20, compared with the case where it is formed only on the surface of the exhaust gas pipe, the surface area substantially in contact with the heat source. And the catalyst layer can be efficiently heated to a high temperature.
【００１８】以上好ましい実施例について説明したが、
本発明は上記実施例に限定されるものではなく、本発明
の要旨を変更しない範囲内において各種の変更が可能で
ある。The preferred embodiment has been described above.
The present invention is not limited to the above embodiments, and various modifications can be made without departing from the spirit of the present invention.
【００１９】[0019]
【発明の効果】以上説明したように、本発明のメタノ−
ルの改質装置は、メタノ−ルの化学反応が起こる反応槽
である多孔質体が熱源である高温流体が流れる手段に直
接接合されており、さらに多孔質体開口部表面に触媒層
が設けられている。したがって、触媒層の熱源への接触
面積が大きいので高温流体から触媒層への熱伝達が効率
よく行われ、触媒層全体が高温に維持されやすく、かつ
多孔質体の開口部を流れるメタノ−ルと触媒層との接触
面積が大きいので、メタノ−ルの還元反応が効率的に行
なわれる。また、本発明のメタノ−ルの改質装置は、反
応槽を構成する多孔質体が高温流体が流れる管の材質の
熱膨脹係数とほぼ等しい熱膨脹係数を有するので、高温
下においても管と多孔質体との接合状態は安定してい
る。さらに、多孔質体の開口部をメタノ−ルが流れるの
で、球状またはペレット状の触媒を用いた場合に比べ
て、圧力損失が小さいのでメタノ−ルを供給するための
駆動ポンプの容量を小さくすることが可能である。As described above, the methanol of the present invention is used.
In the reformer of the reactor, the porous body, which is the reaction tank in which the chemical reaction of methanol occurs, is directly joined to the means through which the high-temperature fluid, which is the heat source, flows, and a catalyst layer is provided on the surface of the opening of the porous body. Has been. Therefore, since the contact area of the catalyst layer with the heat source is large, heat is efficiently transferred from the high temperature fluid to the catalyst layer, the entire catalyst layer is easily maintained at high temperature, and the methanol flowing through the opening of the porous body is Since the contact area between the catalyst layer and the catalyst layer is large, the reduction reaction of methanol is efficiently performed. Further, in the methanol reforming apparatus of the present invention, since the porous body forming the reaction tank has a thermal expansion coefficient substantially equal to the thermal expansion coefficient of the material of the tube through which the high temperature fluid flows, the tube and the porous material are porous even at high temperatures. The state of joint with the body is stable. Further, since the methanol flows through the opening of the porous body, the pressure loss is smaller than that in the case of using a spherical or pellet-shaped catalyst, so that the capacity of the drive pump for supplying the methanol is reduced. It is possible.
【図１】本発明の一実施例のメタノ−ルの改質装置の構
造を示す断面図である。FIG. 1 is a cross-sectional view showing the structure of a methanol reforming apparatus according to an embodiment of the present invention.
【図２】図１のメタノ−ルの改質装置内の反応槽である
円柱型の多孔質体の斜視図である。2 is a perspective view of a cylindrical porous body which is a reaction tank in the methanol reforming apparatus of FIG. 1. FIG.
【図３】図２の多孔質体の管との接合部近傍の様子を示
した拡大図である。FIG. 3 is an enlarged view showing a state in the vicinity of a joint portion of the porous body of FIG. 2 with a tube.
【図４】図３の多孔質体の円Ａ部分の多孔質体表面に設
けられた触媒層の様子を示した拡大図である。FIG. 4 is an enlarged view showing a state of a catalyst layer provided on a surface of a porous body in a circle A portion of the porous body of FIG.
１０ 反応容器 １２、１４ フランジ １６、１７、１８、１９ ボルトおよびナット ２０ 多孔質体 ２２ 開口 ２４ 触媒層 ３０ 気化層 ４０ メタノ−ルの供給口 ４２ メタノ−ルの排出口 ５０ 管 ５２ 銀ろう １００ メタノ−ルの改質装置 ２００、３００ 排気管 10 Reaction Vessel 12, 14 Flange 16, 17, 18, 19 Bolt and Nut 20 Porous Body 22 Opening 24 Catalyst Layer 30 Vaporization Layer 40 Methanol Supply Port 42 Methanol Discharge Port 50 Tube 52 Silver Wax 100 Methano -Reformer 200,300 Exhaust pipe
Claims (5)
段と、前記第１の手段を取り囲んで配設された、メタノ
−ルが流れる流路を形成する第２の手段と、を有するメ
タノ−ルの改質装置において、 前記第２の手段が前記第１の手段に接合された多孔質体
を含み、前記多孔質体の開口部表面にメタノ−ルの化学
反応を進行させるために必要な触媒層を設け、前記高温
流体から前記触媒層への熱伝達率を高めて前記多孔質体
中を流れるメタノ−ルの化学反応効率を向上させるよう
にしたことを特徴とするメタノ−ルの改質装置。1. A first means for forming a flow path through which a high-temperature fluid flows and a second means for forming a flow path through which a methanol flows, which is arranged so as to surround the first means. In the reforming device of methanol, the second means includes a porous body joined to the first means, and a chemical reaction of methanol proceeds on the surface of the opening of the porous body. And a catalyst layer necessary for improving the chemical reaction efficiency of the methanol flowing through the porous body by increasing the heat transfer coefficient from the high temperature fluid to the catalyst layer. Le reformer.
からなり、前記多孔質体が前記管の外壁に接合され、か
つ前記管を構成する材質の熱膨脹係数とほぼ等しい熱膨
脹係数を有する材質からなることを特徴とする請求項１
記載のメタノ−ルの改質装置。2. The coefficient of thermal expansion, wherein the first means comprises one or two or more tubes, the porous body is bonded to an outer wall of the tube, and the coefficient of thermal expansion is substantially equal to the coefficient of thermal expansion of the material forming the tube. 2. A material having
A reforming device for the described methanol.
後に発生するガスを排出するための排出口とを有する反
応容器と、前記反応容器内に収められたメタノ−ルの反
応槽と、前記反応容器を貫通して配設された高温ガスが
流れる１つまたは２つ以上の管と、を有するメタノ−ル
の改質装置において、 前記反応槽が前記反応容器内壁および前記管の外壁に接
合された多孔質体からなり、前記多孔質体の開口部表面
にメタノ−ルの還元反応を進行させるために必要な触媒
層を設け、前記高温ガスから前記触媒層への熱伝達率を
高めて前記多孔質体中を流れるメタノ−ルの還元反応効
率を向上させるようにしたことを特徴とするメタノ−ル
の改質装置。3. A reaction container having a supply port for methanol and a discharge port for discharging gas generated after the reaction of methanol, and a reaction tank for methanol contained in the reaction container. And one or more pipes through which the high-temperature gas flows, which penetrates through the reaction vessel, and wherein the reaction tank has an inner wall of the reaction vessel and a tube. The porous body is joined to the outer wall, and a catalyst layer necessary for advancing the reduction reaction of methanol is provided on the opening surface of the porous body, and the heat transfer coefficient from the high temperature gas to the catalyst layer is provided. To improve the reduction reaction efficiency of the methanol flowing in the porous body.
膨脹係数とほぼ等しい熱膨脹係数を有する材質からなる
ことを特徴とする請求項３記載のメタノ−ルの改質装
置。4. The reforming apparatus for methanol according to claim 3, wherein the porous body is made of a material having a coefficient of thermal expansion substantially equal to that of the material forming the tube.
口と、前記排気ガスの排出口と、メタノ−ルの供給口
と、メタノ−ルの反応後に発生するガスを排出するため
の排出口とを有する反応容器と、前記反応容器内に収め
られたメタノ−ルの反応槽と、前記反応槽を貫通して配
設された、前記排気ガスが流れる１つまたは２つ以上の
管と、を有するデイ−ゼルエンジンの排気管に接合され
たデイ−ゼルエンジン用メタノ−ルの改質装置におい
て、 前記反応槽が前記反応容器内壁および前記管の外壁に接
合された、前記管を構成する材質の熱膨脹係数とほぼ等
しい熱膨脹係数を有する多孔質体からなり、前記多孔質
体の開口部表面に触媒層が設けられ、前記排気ガスから
前記触媒層への熱伝達率を高めて前記多孔質体中を流れ
るメタノ−ルの還元反応効率を向上させるようにしたこ
とを特徴とするデイ−ゼルエンジン用メタノ−ルの改質
装置。5. An inlet for exhaust gas from a diesel engine, an exhaust outlet for the exhaust gas, a supply inlet for methanol, and an exhaust outlet for exhausting gas generated after the reaction of methanol. A reaction vessel having a methanol, a reaction vessel for methanol contained in the reaction vessel, and one or more pipes through which the exhaust gas flows, the tube being disposed so as to penetrate the reaction vessel. In a reformer for a diesel engine methanol joined to an exhaust pipe of a diesel engine, the reaction vessel is joined to an inner wall of the reaction vessel and an outer wall of the pipe, and a material forming the pipe. Of a porous body having a coefficient of thermal expansion substantially equal to that of the porous body, a catalyst layer is provided on the surface of the opening of the porous body, and the heat transfer coefficient from the exhaust gas to the catalyst layer is increased to enhance the porous body. Return of methanol flowing inside A reformer for methanol for diesel engines, which is characterized by improving the original reaction efficiency.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6257673A JPH0891802A (en) | 1994-09-27 | 1994-09-27 | Modifying device of methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6257673A JPH0891802A (en) | 1994-09-27 | 1994-09-27 | Modifying device of methanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0891802A true JPH0891802A (en) | 1996-04-09 |
Family
ID=17309520
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6257673A Pending JPH0891802A (en) | 1994-09-27 | 1994-09-27 | Modifying device of methanol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0891802A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003206105A (en) * | 2002-01-11 | 2003-07-22 | Honda Motor Co Ltd | Catalyst reactor |
| JP2003238111A (en) * | 2002-02-13 | 2003-08-27 | Fuji Seratekku Kk | Apparatus for reforming fuels |
| JP2010105855A (en) * | 2008-10-30 | 2010-05-13 | Rinnai Corp | Reformer and power generation plant |
| US7753971B2 (en) | 2005-03-22 | 2010-07-13 | Toyota Jidosha Kabushiki Kaisha | Fuel reforming apparatus |
-
1994
- 1994-09-27 JP JP6257673A patent/JPH0891802A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003206105A (en) * | 2002-01-11 | 2003-07-22 | Honda Motor Co Ltd | Catalyst reactor |
| JP2003238111A (en) * | 2002-02-13 | 2003-08-27 | Fuji Seratekku Kk | Apparatus for reforming fuels |
| US7753971B2 (en) | 2005-03-22 | 2010-07-13 | Toyota Jidosha Kabushiki Kaisha | Fuel reforming apparatus |
| JP2010105855A (en) * | 2008-10-30 | 2010-05-13 | Rinnai Corp | Reformer and power generation plant |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4358914B2 (en) | Active microchannel heat exchanger | |
| RU2411075C2 (en) | Compact reforming reactor | |
| JP4718069B2 (en) | Compact, lightweight methanol fuel gas autothermal reformer | |
| US6274260B1 (en) | Plant with high temperature fuel cells I | |
| JP4643027B2 (en) | Compact and lightweight self-heating reformer | |
| WO2021221943A1 (en) | Process for the thermal decomposition of ammonia and reactor for carrying out the process | |
| CA2442781A1 (en) | Single chamber compact fuel processor | |
| WO2010087791A1 (en) | Distributively cooled, integrated water-gas shift reactor and vaporizer | |
| US4378336A (en) | Monolith reactor | |
| JP2008543720A (en) | Reformer and reforming method for producing hydrogen from hydrocarbon fuel | |
| US20090258259A1 (en) | Catalytic heat exchangers and methods of operation | |
| US20040005268A1 (en) | Method and multi-stage shift reactor for reducing the carbon monoxide content in a hydrogen-containing gas stream, and reformer installation | |
| US20100086477A1 (en) | Reaction chamber promoting heat exchange between the reagents and the gases that are produced | |
| US6303243B1 (en) | Plant with high temperature fuel cells II | |
| JPH0891802A (en) | Modifying device of methanol | |
| JP4562775B2 (en) | Fine channel heater for uniform heating | |
| US8474240B1 (en) | Regenerative gas generator | |
| JPH0891803A (en) | Modifying device of methanol for engine | |
| US7354465B2 (en) | Device for cooling and humidifying reformate | |
| CN115849302B (en) | Hydrogen production apparatus and method | |
| JP2001220106A (en) | Reformer | |
| JP2000237582A (en) | Device for utilizing heat generated by catalytic reaction | |
| JP2000072405A (en) | Reaction furnace for generating water | |
| JPH0794321B2 (en) | Methanol reforming method using exhaust heat and exhaust heat recovery type methanol reformer | |
| RU2801525C1 (en) | Device for obtaining a hydrogen-containing mixture from ammonia |