JPH0789033B2 - Steam reformer - Google Patents
Steam reformerInfo
- Publication number
- JPH0789033B2 JPH0789033B2 JP60202946A JP20294685A JPH0789033B2 JP H0789033 B2 JPH0789033 B2 JP H0789033B2 JP 60202946 A JP60202946 A JP 60202946A JP 20294685 A JP20294685 A JP 20294685A JP H0789033 B2 JPH0789033 B2 JP H0789033B2
- Authority
- JP
- Japan
- Prior art keywords
- combustion gas
- heat transfer
- catalyst tube
- steam reforming
- catalyst
- 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.)
- Expired - Lifetime
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/003—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by using permeable mass, perforated or porous materials
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Dispersion Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fuel Cell (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Description
【発明の詳細な説明】 〔技術分野〕 本発明は炭化水素と水蒸気を触媒の存在下で高温で気相
反応させる水蒸気改質装置に関するものである。Description: TECHNICAL FIELD The present invention relates to a steam reforming apparatus for reacting a hydrocarbon and steam in a gas phase at a high temperature in the presence of a catalyst.
従来、水蒸気と炭化水素との混合ガスを触媒の存在下で
高温で気相反応させて水素を含む改質ガスを製造する水
蒸気改質方法（steam reforming）は広く知られてい
る。この場合の炭化水素と水蒸気との気相反応は、600
〜900℃という高温の吸熱反応である。この水蒸気改質
方法は、炭化水素と水蒸気との混合ガスを触媒管内を流
通させるとともに、その触媒管の外表面を通常、800〜1
200℃の高温の燃焼ガスと接触させて加熱し、反応に必
要な高温の熱量をその触媒管の管壁を通して内部に入熱
させることによって実施されている。そして、このよう
な水蒸気改質方法は、燃料電池に用いる水素を製造する
ための装置として利用されている。Conventionally, a steam reforming method of producing a reformed gas containing hydrogen by subjecting a mixed gas of steam and hydrocarbon to a gas phase reaction at a high temperature in the presence of a catalyst is widely known. In this case, the gas-phase reaction between hydrocarbon and steam is 600
It is an endothermic reaction at a high temperature of ~ 900 ℃. In this steam reforming method, a mixed gas of hydrocarbon and steam is circulated in the catalyst tube, and the outer surface of the catalyst tube is usually 800 to 1
It is carried out by contacting with a combustion gas at a high temperature of 200 ° C. to heat it, and allowing the amount of high-temperature heat necessary for the reaction to enter the inside through the wall of the catalyst tube. And, such a steam reforming method is used as an apparatus for producing hydrogen used in a fuel cell.
前記水蒸気改質方法を実施するために用いられている一
般的な水蒸気改質装置は、水蒸気と炭化水素との混合ガ
スが管内を流通する触媒管の外表面の一部又は全部を円
筒体で包囲し、その触媒管の外表面と円筒体の内表面と
の間に形成される間隙部に高温燃焼ガスを流通させる構
造のものである。A general steam reforming apparatus used to carry out the steam reforming method is a cylindrical body in which a part or all of the outer surface of a catalyst tube in which a mixed gas of steam and hydrocarbons flows in the tube is formed. The structure is such that the high temperature combustion gas is surrounded and surrounded by a gap formed between the outer surface of the catalyst tube and the inner surface of the cylindrical body.
ところで、従来の水蒸気改質装置においては、高温燃焼
ガスから触媒管の管壁を通して触媒管内に伝達される伝
熱効率が悪いため、水蒸気改質反応に必要な熱量を得る
ために、多量の高温燃焼ガスを必要とし、その結果、水
素の製造コストが高くなるという問題を生じた。By the way, in the conventional steam reforming apparatus, since the heat transfer efficiency of being transferred from the high temperature combustion gas to the inside of the catalyst tube through the wall of the catalyst tube is poor, a large amount of high temperature combustion gas is required to obtain the heat quantity necessary for the steam reforming reaction. Gas is required, and as a result, the production cost of hydrogen increases.
一方、前記伝熱効率を高めるために、環状間隙部にシリ
カ等の耐熱性無機物の粗大粒子（粒径３〜10mm）を充填
することが提案されてる。しかし、この場合にも、その
伝熱効率が未だ満足すべきものではなく、逆に、この場
合には燃焼ガスが環状間隙部を流通する隙の圧力損失が
大きくなるため、燃焼ガスを環状空隙部を流通させるた
めの動力コストが上昇するという問題を生じた。On the other hand, in order to improve the heat transfer efficiency, it has been proposed to fill the annular gap portion with coarse particles (particle diameter 3 to 10 mm) of a heat resistant inorganic material such as silica. However, even in this case, the heat transfer efficiency is not yet satisfactory, and conversely, in this case, the pressure loss in the gap through which the combustion gas flows through the annular gap portion becomes large, so that the combustion gas flows through the annular gap portion. There was a problem that the power cost for distribution would rise.
本発明は、高温燃焼ガスから触媒管内を流通する水蒸気
と炭化水素との混合ガスへの伝熱効率が高く、水素製造
コストの低減された水蒸気改質装置を提供することをそ
の目的とする。It is an object of the present invention to provide a steam reforming apparatus that has high heat transfer efficiency from a high-temperature combustion gas to a mixed gas of steam and hydrocarbons flowing in a catalyst pipe and that reduces hydrogen production cost.
本発明者らは、前記目的を達成すべく鋭意研究を重ねた
結果、高温燃焼ガスに、細線からなる網状体を接触させ
て加熱し、この高温に加熱された網状体から放射される
輻射熱により触媒管を加熱することにより、高温燃焼ガ
スからの触媒管内への伝熱効率を著しく向上し得ること
を見出し、本発明を完成するに至った。As a result of repeated intensive studies to achieve the above-mentioned object, the inventors of the present invention have heated a high temperature combustion gas by bringing a reticulate body made of fine wires into contact with each other, and radiant heat emitted from the reticulated body heated to this high temperature. The inventors have found that heating the catalyst tube can significantly improve the efficiency of heat transfer from the high-temperature combustion gas into the catalyst tube, and have completed the present invention.
即ち、本発明によれば、水蒸気と炭化水素との混合ガス
が管内を流通する触媒管の外表面の一部又は全部を円筒
体で包囲し、該触媒管の外表面と円筒体の内表面との間
に形成される環状間隙部に高温燃焼ガスを流通させる構
造の水蒸気改質装置において、該環状間隙部に、素線の
線径が5mm以下でかつ素線間の間隔が5mm以下である網状
体を輻射伝熱源として配設したことを特徴とする水蒸気
改質装置が提供される。That is, according to the present invention, a part or the whole of the outer surface of the catalyst tube in which the mixed gas of water vapor and hydrocarbon flows in the tube is surrounded by a cylindrical body, and the outer surface of the catalyst tube and the inner surface of the cylindrical body. In a steam reforming device having a structure in which a high-temperature combustion gas is circulated in an annular gap formed between and, in the annular gap, the wire diameter of the wires is 5 mm or less and the distance between the wires is 5 mm or less. There is provided a steam reforming device characterized in that a certain mesh-like body is arranged as a radiant heat transfer source.
次に、本発明を図面により説明する。第１図は、本発明
の水蒸気改質装置の断面説明図を示すもので、１は触媒
管、２は触媒管１の周囲に設けられた円筒体を示す。３
は触媒管１と円筒体２との間に形成される環状間隙部
で、高温燃焼ガスの流路を形成する。触媒管１は、その
内部に水蒸気改質触媒層４を有する。また、この触媒管
１内部は水蒸気と炭化水素ガスの流路を形成する。Next, the present invention will be described with reference to the drawings. FIG. 1 is a cross-sectional explanatory view of a steam reforming apparatus of the present invention, where 1 is a catalyst tube and 2 is a cylindrical body provided around the catalyst tube 1. Three
Is an annular gap portion formed between the catalyst tube 1 and the cylindrical body 2, and forms a flow path for high-temperature combustion gas. The catalyst tube 1 has a steam reforming catalyst layer 4 inside. The inside of the catalyst tube 1 forms a flow path for water vapor and hydrocarbon gas.
本発明においては、高温燃焼ガスの通路を形成する環状
間隙部３内に、網状体Ｍを輻射伝熱源として挿入する。
この場合、網状体Ｍは、円筒形のもので、管体１の外表
面（被加熱面）に沿って、環状間隙部３の中間に配設さ
れる。In the present invention, the mesh body M is inserted as a radiant heat transfer source into the annular gap portion 3 forming the passage for the high temperature combustion gas.
In this case, the mesh body M has a cylindrical shape and is arranged in the middle of the annular gap portion 3 along the outer surface (heated surface) of the tube body 1.
前記装置においては、間隙部３には高温燃焼ガスＡが流
通され、一方、改質触媒層４には水蒸気と炭化水素との
混合ガスＢが流通される。水蒸気と炭化水素との混合ガ
スＢは、改質触媒層４内において反応し、水素を含む改
質ガスが生成される。この反応は高温（約600〜900℃）
の吸熱反応であり、それに必要な熱量は、間隙部３を流
通する高温燃焼ガスから供給される。In the above apparatus, the high temperature combustion gas A is circulated in the gap portion 3, while the mixed gas B of steam and hydrocarbon is circulated in the reforming catalyst layer 4. The mixed gas B of steam and hydrocarbon reacts in the reforming catalyst layer 4 to generate a reformed gas containing hydrogen. This reaction is hot (about 600-900 ℃)
Is an endothermic reaction, and the amount of heat required for it is supplied from the high-temperature combustion gas flowing through the gap 3.
本発明者らの研究によれば、前記のような構造の水蒸気
改質装置においては、その網状体Ｍを輻射伝熱源として
配設したことにより、伝熱効率が著しく高められること
が見出された。この伝熱効率の向上は、次のような理由
によるもとの考えられる。即ち、網状体の場合、細線で
構成され、かつ比表面積が大きく、しかも高温燃焼ガス
の通路の中間に配設されていることから、その網状体全
体は、高温燃焼ガスにより容易に高温に加熱され、その
表面温度は、燃焼ガスの温度と近い高温となる。このよ
うな表面温度が高く、しかも比表面積の大きな網状体
は、大きな熱輻射能を有し、その輻射伝熱によって触媒
管外表面は高温度に加熱され、触媒管内への入熱量も大
きくなる。触媒管外表面は燃焼ガスと接触していること
から、触媒管内には、この接触加熱による入熱も存在す
るが、その割合は小さく、触媒管内への入熱の大部分
（約80％以上）は、前記網状体からの輻射伝熱量であ
る。その結果、高温燃焼ガスからの触媒管１の外表面へ
の全体的な熱伝達は、網状体を用いない場合の熱伝達に
比して、著しく大きくなる。According to the research conducted by the present inventors, it has been found that in the steam reforming apparatus having the above-mentioned structure, the heat transfer efficiency is remarkably enhanced by disposing the mesh body M as a radiation heat transfer source. . This improvement in heat transfer efficiency is considered to be due to the following reasons. That is, in the case of a mesh, since it is composed of fine wires, has a large specific surface area, and is arranged in the middle of the passage of the high temperature combustion gas, the whole mesh is easily heated to a high temperature by the high temperature combustion gas. As a result, the surface temperature becomes high, which is close to the temperature of the combustion gas. Such a reticulate body having a high surface temperature and a large specific surface area has a large heat radiation ability, and the radiation heat transfer heats the outer surface of the catalyst tube to a high temperature, thereby increasing the heat input into the catalyst tube. . Since the outer surface of the catalyst tube is in contact with the combustion gas, there is also heat input due to this contact heating inside the catalyst tube, but the proportion is small, and most of the heat input into the catalyst tube (about 80% or more) ) Is the amount of radiant heat transfer from the mesh. As a result, the overall heat transfer from the hot combustion gases to the outer surface of the catalyst tube 1 is significantly greater than that without the mesh.
本発明で用いる網状体において、その素線の材質は耐熱
性を有するものであれば任意であるが、一般には、ニッ
ケル・クロム等の金属線やセラミックス線等が用いられ
る。網状体を形成する素線の線径は、できるだけ細線の
方が好ましいが、一般には、直径5mm以下、好ましくは
１〜3mm程度のものが用いられる。網状体の織型として
は、平織、綾織、平畳織、綾畳織、莚織、バランス織、
ヘリンボーン織等があり、各素線間の間隔は、5mm以
下、好ましくは１〜3mm程度である。前記輻射伝熱は、
網状体を構成する素線の線径や素線間の間隔により影響
され、素線が大きすぎると網状体の単位重量当りの表面
積が小さくなるため、効率的な輻射伝熱が得られなくな
り、また、素線間の間隔が大きすぎると、網状体の単位
面積当りの素線密度が小さくなるため、効率的な輻射伝
熱が得られなくなる。網状体を触媒管１の外表面に沿っ
て環状間隙部に配設する場合、高温燃焼ガスの圧力損失
を増加させないようガス流路断面積の1/3〜1/5程度に配
設することが好ましい。In the reticulate body used in the present invention, the material of the element wire is arbitrary as long as it has heat resistance, but in general, a metal wire such as nickel / chrome or a ceramic wire is used. The wire diameter of the wire forming the net-like body is preferably as thin as possible, but in general, a wire having a diameter of 5 mm or less, preferably about 1 to 3 mm is used. As the woven type of the net-like body, plain weave, twill weave, flat tatami weave, twill tatami weave, edible weave, balanced weave,
Herringbone weave and the like are used, and the distance between the individual wires is 5 mm or less, preferably about 1 to 3 mm. The radiant heat transfer is
Affected by the wire diameter of the wires forming the mesh and the spacing between the wires, the surface area per unit weight of the mesh is too small if the wires are too large, and efficient radiation heat transfer cannot be obtained. Further, if the spacing between the strands is too large, the strand density per unit area of the reticulate body becomes small, so that efficient radiation heat transfer cannot be obtained. When the reticulate body is arranged in the annular gap along the outer surface of the catalyst tube 1, it should be arranged in about 1/3 to 1/5 of the gas flow passage cross-sectional area so as not to increase the pressure loss of the high temperature combustion gas. Is preferred.
前記環状間隙部３には、耐火性無機物（セラミックス）
のボールやラシッヒリング等の充填材を充填し、これに
よって伝熱能を高めることも可能であるが、この場合に
は、網状体の場合とは異なり、伝熱能を高めようとする
と、高温燃焼ガスが環状間隙部３を流通する際の圧力損
失が大きくなるという欠点を有する。即ち、伝熱能を高
めようとすると充填材の粒子径を小さくすることが必要
となる。一方、充填材の粒子径を小さくすると、環状間
隙部３における充填材の充填は密充填になり、圧力損失
が大きくなる。しかも、間隙部３に充填材を充填した充
填層では伝熱を行うことより円周方向に温度分布が生
じ、触媒管１の表面に近い方の充填材の温度が低く、触
媒管１の表面から遠い方の充填材の温度が高くなる。こ
れに対し、網状体を環状間隙部３の中間に配設する時に
は、前記のような欠点は生じない。The annular gap 3 has a refractory inorganic material (ceramics).
It is possible to fill the ball with a filler such as balls or Raschig rings to increase the heat transfer capacity, but in this case, unlike the case of the mesh body, when trying to increase the heat transfer capacity, high temperature combustion gas It has a drawback that the pressure loss when flowing through the annular gap portion 3 becomes large. That is, in order to improve the heat transfer ability, it is necessary to reduce the particle size of the filler. On the other hand, when the particle size of the filler is reduced, the filler in the annular gap portion 3 is densely packed, and the pressure loss increases. Moreover, in the packed bed in which the gap 3 is filled with the filler, heat transfer causes a temperature distribution in the circumferential direction, the temperature of the filler near the surface of the catalyst tube 1 is low, and the surface of the catalyst tube 1 is low. The temperature of the filler farther away from is higher. On the other hand, when the net-like body is arranged in the middle of the annular gap portion 3, the above-mentioned drawback does not occur.
本発明の水蒸気改質装置において、環状間隙部３には、
高温燃焼ガスの流路の途中に、その流路断面積を狭める
１個又は複数の工作物を設け、間隙部３内を通る高温燃
焼ガスに乱れを生じさせ、伝熱効率をさらに向上させる
ことができる。この場合、工作物の配置は、流路断面積
を狭める方法であれば任意であり、例えば、触媒管１の
外表面や、円筒体２の内表面に隆起物を配設する方法の
他、触媒管１を包囲する環状リングを配設する方法等が
ある。In the steam reforming apparatus of the present invention, the annular gap portion 3 has
One or more workpieces that narrow the cross-sectional area of the flow path of the high temperature combustion gas are provided in the middle of the flow path of the high temperature combustion gas to cause turbulence in the high temperature combustion gas passing through the gap portion 3 and further improve the heat transfer efficiency. it can. In this case, the arrangement of the workpiece is arbitrary as long as it is a method of narrowing the flow passage cross-sectional area. For example, other than the method of disposing the protrusion on the outer surface of the catalyst tube 1 or the inner surface of the cylindrical body 2, There is a method of arranging an annular ring surrounding the catalyst tube 1.
第２図（ａ）に、環状リングを間隙部３に配設した場合
の説明断面図を示す。第２図（ｂ）は環状リングの平面
図を示す。FIG. 2A shows an explanatory cross-sectional view when the annular ring is arranged in the gap portion 3. FIG. 2 (b) shows a plan view of the annular ring.
第２図において、10は環状リングであり、この環状リン
グは板状連結体11によって各連結されて、間隙部３内に
配設されている。この環状リングの配設により、間隙部
３の高温燃焼ガス流路は、それら環状リングの配設位置
において狭くなり、高温燃焼ガスの流れに乱れが生じ
る。この環状リングは網状体の支持体として用いること
ができ、第２図においては、環状リングの内側に、網状
体Ｍは、スポット溶接により固着されている。また、こ
の環状リングは、その間隙部３内への配設が容易なよう
に、半割又は３つ割部材として配設することも可能であ
る。なお、第２図には、環状リングの間隙部３内への固
定法については図示されていないが、この環状リング
は、触媒管１上部に支持棒を固着し、この支持棒にフッ
クを介してその全体を吊り下げたり、あるいは連結体を
介して、環状リングを触媒管１の表面に固定させる等し
て、間隙部３内に配設することができる。In FIG. 2, reference numeral 10 denotes an annular ring, which are connected to each other by a plate-like connecting body 11 and are arranged in the gap 3. By disposing the annular ring, the high temperature combustion gas passage in the gap portion 3 becomes narrow at the disposition position of the annular rings, and the flow of the high temperature combustion gas is disturbed. This annular ring can be used as a support for the mesh-like body. In FIG. 2, the mesh-like body M is fixed to the inside of the annular ring by spot welding. Further, this annular ring can be arranged as a half-divided member or a three-divided member so that the annular ring can be easily arranged in the gap 3. Although the method of fixing the annular ring in the gap 3 is not shown in FIG. 2, this annular ring has a support rod fixed to the upper portion of the catalyst tube 1 and a hook attached to the support rod. It can be disposed in the gap portion 3 by suspending the whole thereof, or by fixing the annular ring to the surface of the catalyst tube 1 via a connecting body.
次に、本発明を実施例によりさらに詳細に説明する。 Next, the present invention will be described in more detail with reference to examples.
実施例 加熱された網状体による輻射伝熱効率を調べるために以
下の実験を行った。Example The following experiment was conducted in order to investigate the radiation heat transfer efficiency by the heated mesh.
実験装置として、スチール製の２重管構造の装置を用い
た。この場合、内管は、外径22cm、長さ75cmのものであ
り、外管は、内径25cm、長さ75cmのものである。この２
重管の内管外表面と外管内表面との間の間隔は、15mmで
あり、この内管と外管との空隙部の中間の位置には、直
径1.1mmの合金鋼製細線を平織した金網（金属線相互の
間隔:2.5mm）を直径23.5cmの円筒状に成形して挿入し
た。As a test device, a device having a double tube structure made of steel was used. In this case, the inner tube has an outer diameter of 22 cm and a length of 75 cm, and the outer tube has an inner diameter of 25 cm and a length of 75 cm. This 2
The distance between the outer surface of the inner pipe and the inner surface of the outer pipe of the heavy pipe was 15 mm, and an alloy steel fine wire with a diameter of 1.1 mm was plain-woven at a position midway between the voids of the inner pipe and the outer pipe. A wire mesh (interval between metal wires: 2.5 mm) was formed into a cylindrical shape having a diameter of 23.5 cm and inserted.
このような２重管構造の装置に対し、内管に冷空気を流
通させ、外管と内管との間の環状間隙部に温度850℃に
加熱した燃焼ガスを種々の速度で流通させ、燃焼ガスか
ら内管表面への熱伝熱を行わせた。この場合の燃焼ガス
からの内管表面への熱伝熱を測定し、その結果を、見掛
伝熱係数として表−１に示す。With respect to such a device having a double pipe structure, cold air is circulated in the inner pipe, and combustion gas heated to a temperature of 850 ° C. is circulated at various speeds in an annular gap portion between the outer pipe and the inner pipe. Heat was transferred from the combustion gas to the inner tube surface. In this case, heat transfer from the combustion gas to the inner pipe surface was measured, and the result is shown in Table-1 as an apparent heat transfer coefficient.
実施例２ 実施例１において、内管内に、改質触媒として、アルミ
ナに担持させたニッケル触媒（平均粒径:5mm）を充填
し、高さが40cmの触媒層を形成するとともに、内管内を
流通させるガスとして、水蒸気19.8Nm3/hと炭化水素
（メタン）6.6Nm3/hとの混合ガスを用いた以外は同様に
して実験を行った。この場合の混合ガスの空間速度（GH
SV）は300/hである。その結果を表−２に示す。 Example 2 In Example 1, the inner tube was filled with a nickel catalyst (average particle size: 5 mm) supported on alumina as a reforming catalyst to form a catalyst layer having a height of 40 cm. The same experiment was performed except that a mixed gas of steam 19.8 Nm 3 / h and hydrocarbon (methane) 6.6 Nm 3 / h was used as the gas to be circulated. Space velocity of mixed gas in this case (GH
SV) is 300 / h. The results are shown in Table-2.
〔効 果〕 表−１に示した結果から、本発明の網状体を設置した水
蒸気改質装置は、従来の網状体を環状間隙部に設置しな
いものに比べ、燃焼ガスから円管表面への熱伝達効率が
著しく向上したことがわかる。 [Effects] From the results shown in Table 1, the steam reforming apparatus having the reticulated body of the present invention installed from the combustion gas to the surface of the circular pipe compared to the conventional reticulated body not having the reticulated body installed in the annular gap. It can be seen that the heat transfer efficiency is significantly improved.
また、表−２に示した結果から、内管外表面への熱伝達
効率の向上とともに、内管内を流通する水蒸気／炭化水
素混合ガスの温度が上昇するため、水蒸気改質反応の平
衡が生成物側に傾き、得られる改質ガス中の水素濃度が
増加することがわかる。これらのことから、本発明の水
蒸気改質方法及び装置によれば、低められたコストで水
素を製造し得ることが明らかである。Further, from the results shown in Table-2, the efficiency of heat transfer to the outer surface of the inner pipe is improved, and the temperature of the steam / hydrocarbon mixed gas flowing in the inner pipe is increased, so that equilibrium of the steam reforming reaction is generated. It can be seen that the hydrogen concentration in the obtained reformed gas increases as it tilts toward the product side. From these, it is apparent that the steam reforming method and apparatus of the present invention can produce hydrogen at a reduced cost.
第１図は、水蒸気改質装置の断面説明図である。第２図
（ａ）は、触媒管と円筒体との間に形成される間隙部に
環状リングを配設した場合の説明断面図であり、第２図
（ｂ）はその平面図である。 １……触媒管、２……円筒体、３……間隙部、４……触
媒層、10……環状リング、11……板状連結体、Ｍ……網
状体。FIG. 1 is a cross-sectional explanatory view of a steam reforming apparatus. FIG. 2 (a) is an explanatory cross-sectional view in the case where an annular ring is arranged in the gap formed between the catalyst tube and the cylindrical body, and FIG. 2 (b) is a plan view thereof. DESCRIPTION OF SYMBOLS 1 ... Catalyst tube, 2 ... Cylindrical body, 3 ... Gap, 4 ... Catalyst layer, 10 ... Annular ring, 11 ... Plate connection body, M ... Mesh body.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 酒井 直樹 神奈川県横浜市金沢区釜利谷町2263―27 (72)発明者 渋沢 満 神奈川県横浜市旭区若葉台４−13―902 (72)発明者 太田 増夫 神奈川県横浜市緑区竹山４−２ (72)発明者 浜田 紀文 神奈川県川崎市中原区田尻町77 (72)発明者 平林 俊彦 兵庫県神戸市兵庫区和田崎町１−１―２ 三菱電機株式会社神戸製作所内 (56)参考文献 特開 昭58−33091（ＪＰ，Ａ) 特開 昭58−23168（ＪＰ，Ａ) 特開 昭59−10341（ＪＰ，Ａ) 特公 昭39−21195（ＪＰ，Ｂ１) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Naoki Sakai 2263-27, Kamariya-cho, Kanazawa-ku, Yokohama-shi, Kanagawa (72) Inventor Mitsuru Shibusawa 4-13-902, Wakabadai, Asahi-ku, Yokohama-shi, Kanagawa (72) Ota Masuo 4-2 Takeyama, Midori-ku, Yokohama-shi, Kanagawa 72 Inventor Kibun Hamada 77 Tajiri-cho, Nakahara-ku, Kawasaki-shi, Kanagawa 77 (72) Toshihiko Hirabayashi 1-2-2, Wadazaki-cho, Hyogo-ku, Kobe-shi, Hyogo Mitsubishi Electric (56) Reference JP 58-33091 (JP, A) JP 58-23168 (JP, A) JP 59-10341 (JP, A) JP 39-21195 ( JP, B1)
Claims (1)
通する触媒管の外表面の一部又は全部を円筒体で包囲
し、該触媒管の外表面と円筒体の内表面との間に形成さ
れる環状間隙部に高温燃焼ガスを流通させる構造の水蒸
気改質装置において、該環状間隙部に、素線の線径が5m
m以下でかつ素線間の間隔が5mm以下である網状体を輻射
伝熱源として配設したことを特徴とする水蒸気改質装
置。1. A part or all of the outer surface of a catalyst tube in which a mixed gas of water vapor and hydrocarbons flows is surrounded by a cylinder, and the space between the outer surface of the catalyst tube and the inner surface of the cylinder. In the steam reforming device having a structure in which the high-temperature combustion gas is circulated in the annular gap formed in, the wire diameter of the wire is 5 m in the annular gap.
A steam reforming device, characterized in that a mesh body having a length of m or less and a distance between the wires of 5 mm or less is provided as a radiant heat transfer source.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60202946A JPH0789033B2 (en) | 1985-09-13 | 1985-09-13 | Steam reformer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60202946A JPH0789033B2 (en) | 1985-09-13 | 1985-09-13 | Steam reformer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6262193A JPS6262193A (en) | 1987-03-18 |
| JPH0789033B2 true JPH0789033B2 (en) | 1995-09-27 |
Family
ID=16465780
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60202946A Expired - Lifetime JPH0789033B2 (en) | 1985-09-13 | 1985-09-13 | Steam reformer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0789033B2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01157974U (en) * | 1988-04-12 | 1989-10-31 | ||
| JPH02160077A (en) * | 1988-12-15 | 1990-06-20 | Dainippon Printing Co Ltd | Decorative material manufacturing method and manufacturing equipment |
| EP2591851A1 (en) * | 2011-11-08 | 2013-05-15 | Alfa Laval Corporate AB | A tube module |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5833091A (en) * | 1981-08-22 | 1983-02-26 | Agency Of Ind Science & Technol | Double pipe type heat exchanger |
-
1985
- 1985-09-13 JP JP60202946A patent/JPH0789033B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6262193A (en) | 1987-03-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP7395482B2 (en) | Solid-filled equipment for carrying out endothermic reactions with direct electrical heating | |
| CN105188903B (en) | Radiant walls catalytic reactor and the method for implementing chemical reaction in this reactor | |
| JP2592662B2 (en) | Implementation of heterogeneous catalytic chemical processes | |
| JP2021525697A (en) | Steam reforming heated by resistance heating | |
| JP2005519832A5 (en) | ||
| JP2005519832A (en) | Induction heating reactor for gas phase catalytic reactions | |
| JP2019532904A (en) | Catalyst tube for reforming | |
| JP5443173B2 (en) | Cylindrical steam reformer | |
| KR100474612B1 (en) | Inductively Heated Catalytic Reactor | |
| JPH0789033B2 (en) | Steam reformer | |
| TW202027853A (en) | Catalyst particle shape | |
| US3899420A (en) | Steam reformer for hydrocarbons | |
| US2397899A (en) | Process and apparatus for performing endothermic catalytic reactions in the gas phase | |
| RU2193918C2 (en) | Method of induction initiation of chemical reaction | |
| JPS62216634A (en) | fuel reformer | |
| JPH08301602A (en) | Fuel reformer | |
| JPH0124533B2 (en) | ||
| JPH0673627B2 (en) | Reactor | |
| RU2232045C1 (en) | Reactor for a direct synthesis of organochlorosilane in a boiling bed | |
| JPH08225301A (en) | Methanol reformer | |
| CN120393920A (en) | Reforming reaction system based on Joule heating effect and its application | |
| JPS58124532A (en) | Endothermic reaction apparatus | |
| JPH0530497B2 (en) | ||
| JPH11179190A (en) | Reformer | |
| JPS62138302A (en) | Device for reforming fuel for fuel cell |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| EXPY | Cancellation because of completion of term |