JPS6061544A - Vertical reactor for methanol manufacture - Google Patents

Vertical reactor for methanol manufacture

Info

Publication number
JPS6061544A
JPS6061544A JP17422284A JP17422284A JPS6061544A JP S6061544 A JPS6061544 A JP S6061544A JP 17422284 A JP17422284 A JP 17422284A JP 17422284 A JP17422284 A JP 17422284A JP S6061544 A JPS6061544 A JP S6061544A
Authority
JP
Japan
Prior art keywords
reactor
heat exchange
tube
catalyst bed
cylindrical jacket
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
Application number
JP17422284A
Other languages
Japanese (ja)
Other versions
JPH0437809B2 (en
Inventor
フロームート・フオルハルト
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
MAN AG
Original Assignee
MAN Maschinenfabrik Augsburg Nuernberg AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by MAN Maschinenfabrik Augsburg Nuernberg AG filed Critical MAN Maschinenfabrik Augsburg Nuernberg AG
Publication of JPS6061544A publication Critical patent/JPS6061544A/en
Publication of JPH0437809B2 publication Critical patent/JPH0437809B2/ja
Granted legal-status Critical Current

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496Heating or cooling the reactor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008Controlling the process
    • B01J2208/00017Controlling the temperature
    • B01J2208/00106Controlling the temperature by indirect heat exchange
    • B01J2208/00115Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132Tubes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18Details relating to the spatial orientation of the reactor
    • B01J2219/185Details relating to the spatial orientation of the reactor vertical

Abstract

(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。
(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

【発明の詳細な説明】 産業上の利用分野 本発明は、ハウジング内部にある触媒床を貫通する熱交
換管をもつ円筒状ハウジングと、反応器下部にあって触
媒床を支えるガス透過底または網とを有する、メタノー
ルの製造用直立反応器に関する。
DETAILED DESCRIPTION OF THE INVENTION Industrial Application The present invention comprises a cylindrical housing with heat exchange tubes passing through a catalyst bed inside the housing and a gas permeable bottom or mesh in the lower part of the reactor supporting the catalyst bed. The present invention relates to an upright reactor for the production of methanol, comprising:

従来技術 このような反応器は多様な形で公知である。Conventional technology Such reactors are known in various forms.

例えばドイツ連邦共和国特許出願公開第3007203
号明細書は、円筒状ハウジング、この円筒状ハウジング
内に設けられる触媒材料からなる随屑、およびとのM:
積の中に延びて冷却液体を導く熱交換管をもつ触媒によ
るメタノール合成用反応器を記載しており、雉積中の熱
交換管は直線状に形成され、ハウジング軸線に対してほ
ぼ平行に延びている。低いガス側圧方効果で充分な加熱
面密度を得るため、熱交換管はひれをσ11えている。
For example, Federal Republic of Germany Patent Application No. 3007203
The patent specification discloses a cylindrical housing, a scrap consisting of a catalyst material provided within the cylindrical housing, and M:
describes a reactor for catalytic methanol synthesis having heat exchange tubes extending into the tube and conducting a cooling liquid, the heat exchange tubes in the tube being straight and running approximately parallel to the housing axis. It is extending. In order to obtain sufficient heating surface density with a low gas side pressure effect, the fins of the heat exchange tubes are increased by σ11.

発明の目的 最初にあげたような公知のメタノール反応器に対し、本
発明の課題は、充填触媒の交換や触媒床中の熱交換管の
監視および交換や触媒床の底または網の交代も構造的に
簡屯な反応器FXI成で容易に行なうことのできる反応
器を提供することにある。前にあげたこれらの要求にも
かかわらず、同じ目的のための公知の熱交換管よりも長
い寿命を得るため、触媒床内の流れ駄軛を改善する。
Purpose of the Invention With respect to the known methanol reactor as mentioned at the beginning, the present invention has a problem of replacing the packed catalyst, monitoring and replacing the heat exchange tubes in the catalyst bed, and changing the structure of the bottom or the mesh of the catalyst bed. The object of the present invention is to provide a reactor that can be easily carried out using a relatively simple reactor FXI construction. Despite these requirements listed above, it improves the flow sag within the catalyst bed in order to obtain a longer life than known heat exchange tubes for the same purpose.

目的を達するための手段 この課題を解法するため本発明によれば、ハウジングが
上にある堵体により閉鎖され、ハウジング内にあって触
媒床を包囲する円筒状外被が、ll’l″1体を取外し
て触媒床と共に反応器の縦方向にそのハウジングから取
出し可能である。
Means for achieving the object In order to solve this problem, according to the invention, the housing is closed by an overlying catalyst body, and a cylindrical jacket, located inside the housing and surrounding the catalyst bed, is provided. The body can be removed and removed along with the catalyst bed from its housing in the longitudinal direction of the reactor.

特許請求の範IJ11の実施態様順は、特γ「請求の範
囲第1項の特徴の展開と改良に役だつ。
The order of implementation of claim IJ11 is particularly useful for developing and improving the features of claim 1.

公開の効果 本発明による反応器の利点は、なるべくひれ付き管から
なる円筒状外被を、充填制!奴と共にハウジングからそ
の中間部分である圧力外被と絶縁外被とで閉鎖して取外
し、それから触媒を円筒状外被から自由に下方へ出すた
め、触媒床の床または網を全部または一部外しさえすれ
ばよいことである。触媒床の底または網を再び閉じれば
、なるべくひれ付き管からなる円筒状外被への触媒材料
の充填を行なうことができる。
Effects of disclosure The advantage of the reactor according to the present invention is that the cylindrical jacket, preferably made of a finned tube, is packed! The intermediate portions of the pressure jacket and the insulation jacket are removed from the housing along with the enclosure, and then the bed or mesh of the catalyst bed is removed in whole or in part to allow the catalyst to freely exit downwardly from the cylindrical jacket. All you have to do is do it. When the bottom of the catalyst bed or the screen is closed again, the cylindrical envelope, preferably consisting of finned tubes, can be filled with catalyst material.

同じことが熱交換管の交換についてもいえる。The same is true for replacing heat exchange tubes.

これらの熱交換管は触媒のハウジングから除去する必要
がなく、容易に接近して全断面にわたって上に開いた円
筒状外被から個々に取外すかまたはこの中へ組込むこと
ができ、る。熱交換管の間に均一な幾何学的流れ空間を
形成し、これらの空間を閉じて隣接する空間へのガスの
漂遊を防止し、これにより熱交換管への均一な作用を行
なうことによって、触媒床内における流れ状朗が改善さ
れる。熱交換器において特に新しい分解ガスおよび(ま
たは)−合成ガスを冷却するため、熱交換管にひれを設
けて、閉じた幾何学的空間を形成することは、ドイツ連
邦共和国特許出願公開第1501640号明細・廚から
公知である。これに対し本発明による反応器は、熱交換
管の間の空間が触媒材料の収容空間として用いられると
いう点で相違している。
These heat exchange tubes do not have to be removed from the catalyst housing, but can be easily accessed and removed individually from or integrated into the cylindrical jacket, which is open at the top over its entire cross section. By creating uniform geometric flow spaces between the heat exchange tubes and closing these spaces to prevent the straying of gas into adjacent spaces, thereby providing a uniform action on the heat exchange tubes, Flow conditions within the catalyst bed are improved. The provision of heat exchange tubes with fins to form closed geometrical spaces, in particular for cooling fresh cracked gas and/or synthesis gas in a heat exchanger, is disclosed in German Patent Application No. 1501640. It is publicly known from the specification. The reactor according to the invention, on the other hand, differs in that the space between the heat exchange tubes is used as a storage space for the catalyst material.

流れ空間へ突出するピンをもつひれ付き熱交換管の利点
は、ピンより下の触媒材料がピンより上の触媒材料、の
重量による荷重を受けず、これにより触媒材料の隙間が
形成され、それにより触媒床内における流れ状轢が改善
されることである。さらに管にあるピンは触媒材料から
管したがって熱交換媒体への熱伝達を高めるのに役だつ
The advantage of finned heat exchange tubes with pins projecting into the flow space is that the catalytic material below the pins is not loaded by the weight of the catalytic material above the pins, which creates gaps in the catalytic material that This improves the flow condition within the catalyst bed. Additionally, the pins in the tubes serve to enhance heat transfer from the catalyst material to the tubes and thus to the heat exchange medium.

壁例えば溶融室の壁にピンを設けて、溶融室の突き固め
材料または内張りを支持しかつ医持すること自体は公知
である。したがってここには本発明とは異なる課題およ
び効果がある。
It is known per se to provide pins in walls, for example of melting chambers, to support and protect the tamping material or lining of the melting chamber. Therefore, there are problems and effects different from those of the present invention.

本発明による反応器はメタノールの製造に適するのみな
らず、その中で他の触媒反応を実施することもできる。
The reactor according to the invention is not only suitable for the production of methanol, but also other catalytic reactions can be carried out therein.

実施例 口部には本発明による反応器の実施例が示されている。Example An embodiment of the reactor according to the invention is shown at the mouth.

第1図による直立反応器の実施例では、そのハウジング
Gは外側の円筒状圧力外被lをもち、この圧力外被1は
反応器の上部から下部へ延び、その上縁および下縁にそ
れぞれフランジ2,3をもっている。ハウジングGを上
方に対して閉鎖する帽体4は、そのフランジ5により円
筒状圧力外被lのフランジ2と結合され、ハウジングG
の底6はそのフランジ7によりフランジ3と結合されて
いる。
In the embodiment of the upright reactor according to FIG. 1, the housing G has an outer cylindrical pressure jacket 1 extending from the top to the bottom of the reactor and at its upper and lower edges, respectively. It has flanges 2 and 3. A cap 4, which closes the housing G from above, is connected by its flange 5 to the flange 2 of the cylindrical pressure jacket l, and
The bottom 6 of is connected to the flange 3 by its flange 7.

圧力外被1を内張すする絶縁外被としての絶縁層8は、
フランジ2,5の分疏面からフランジ3.7の分子a而
へ達している。帽体4および底6も絶w層9.10で内
張すされている。圧力外被1および副体4または底6と
その内張りは、帽体4を圧力外被lから困難なしに除去
できるように構成されている。必要な場合同じことが底
6についてもいえる。
The insulating layer 8 as an insulating jacket lining the pressure jacket 1 is:
It reaches the molecule a of the flange 3.7 from the split surface of the flanges 2 and 5. The cap body 4 and the bottom 6 are also lined with a thin layer 9.10. The pressure jacket 1 and the secondary body 4 or bottom 6 and its lining are configured in such a way that the cap 4 can be removed from the pressure jacket I without difficulty. The same is true for base 6 if necessary.

円筒状圧力外被1を内張すする絶縁層8は、熱交換器1
1の中間部分を収容している。この熱交換器11はその
処周を閉じられてひれ付き管12から形成される円筒状
外被13をもっている。ひれ4=Jき管12の上端およ
び下端は太くされた管部分14.15へ通じ、これらの
管部分】4゜15は下の分配環状導管16および上の集
合環状導管17へ通じている。熱交換器1】用の冷却媒
体は、第1図による実施例では底6およびその絶縁層1
0を貫通する1つまたは複数の管18を経て供給され、
一方篇度上昇した冷却媒体は集合環状導管17から1つ
または複数の菅19を経て取出される。
An insulating layer 8 lining the cylindrical pressure jacket 1 is a heat exchanger 1
It houses the middle part of 1. The heat exchanger 11 has a cylindrical jacket 13 closed around its periphery and formed from a finned tube 12 . The upper and lower ends of the fin 4=J tube 12 lead into thickened tube sections 14.15, these tube sections 4.15 leading into the lower distribution annular conduit 16 and the upper collecting annular conduit 17. In the embodiment according to FIG.
supplied via one or more tubes 18 passing through the
On the other hand, the increased cooling medium is taken out from the collection annular conduit 17 via one or more pipes 19.

円筒状外被13のひれ付き管12の太くされた管部分1
4および15には、反応器の縦軸線に対して平行に垂直
に延びる熱交換1111の熱交換管22の水平面内に延
びる端部20,2+が通じているので、熱交換管の管束
が形成される。
Thickened tube section 1 of finned tube 12 of cylindrical jacket 13
4 and 15 communicate with the ends 20, 2+ extending in the horizontal plane of the heat exchange tubes 22 of the heat exchanger 1111, which extend perpendicularly and parallel to the longitudinal axis of the reactor, so that a tube bundle of heat exchange tubes is formed. be done.

環状導管16の高さの所または第1図に示すようにこの
環状導管16の少し上の所に、この環状導管16の内側
自白断面にわたってまたは管部分15の間に触媒床の網
または底23が延び、その」−に截る触■材料は管22
の間にあり、触媒床の網または底23からほぼフランジ
2.5の分離面の高さの所まで延びている。
At the level of the annular conduit 16 or slightly above this annular conduit 16 as shown in FIG. The material is the tube 22.
It extends from the net or bottom 23 of the catalyst bed approximately to the level of the separation surface of the flange 2.5.

底6はその絶縁層lOと共に原料ガス供給導管24をも
ち、一方帽体4はその内張り9と共にメタノールを出し
導管25をもっている。原訃1ガスは管22とこれらの
管22の訪げられた端部20,21との間の触媒床26
を通って流れて、触媒による反応後メタノールガスとし
て管25を通して導出される。
The bottom 6, together with its insulating layer 1O, has a source gas supply conduit 24, while the cap 4, together with its lining 9, has a methanol discharge conduit 25. The raw material gas flows through the catalyst bed 26 between the tubes 22 and the visited ends 20, 21 of these tubes 22.
After reaction with the catalyst, it is discharged as methanol gas through pipe 25.

周囲を閉じられてひれ付き管12からなる円筒状外被】
3は、反応器の絶縁層8に密接している。帽体4をその
絶縁層9と共に外すと、熱交換器】1をその外被13お
よび触媒材料と共に反応器から上方へ除去することがで
きる。それから触媒床の網または底23を一部または全
部外すことにより、触媒材料を外被13から取出して交
換することができる。熱交換器11の管は、ハウジング
G外で容易に上方または下方へ円筒状外被13から取外
すかまたはこの中へ組込むことができる。
A cylindrical jacket whose circumference is closed and consists of a finned tube 12]
3 is in close contact with the insulating layer 8 of the reactor. Once the cap 4 with its insulating layer 9 has been removed, the heat exchanger 1 together with its jacket 13 and catalyst material can be removed upwards from the reactor. The catalyst material can then be removed from the jacket 13 and replaced by partially or completely removing the catalyst bed screen or bottom 23. The tubes of the heat exchanger 11 can be easily removed from the cylindrical jacket 13 or integrated into it, either upwardly or downwardly, outside the housing G.

第2図による実施例でも外側子方外被51が設けられ、
絶縁層52により内張すされている。
In the embodiment according to FIG. 2, an outer child jacket 51 is also provided,
It is lined with an insulating layer 52.

外被51は帽体55のフランジ55と結合可能なフラン
ジ53をもっている。原料ガスの供給は、圧力外被51
およびその絶縁層52を貫通する反応器のほぼ中間の高
さの所にある導管56により行なわれる。絶縁層52は
第1図による実施例におけるのと同じように熱交換器を
包囲している。熱交換器はひれ付き管58からなる力側
円筒状外被57をもち、これらのひれ付き管58は導管
56の高さの所で切欠かれているので、原料ガスは外被
57の内部へ入ることができる。
The jacket 51 has a flange 53 that can be combined with a flange 55 of the cap body 55. The raw material gas is supplied through the pressure envelope 51.
and by a conduit 56 at about mid-height of the reactor which penetrates the insulating layer 52. An insulating layer 52 surrounds the heat exchanger as in the embodiment according to FIG. The heat exchanger has a power-side cylindrical jacket 57 consisting of fin tubes 58 which are cut out at the level of the conduits 56 so that the feed gas can flow into the interior of the jacket 57. You can enter.

第2図においても、端部59,60を冊げられて管束に
まとめられる熱交換管61が設けられて、ひれ付き管5
8の太くされた部分62.63へ通じ、一方これらの部
分62.63が通ずる環、状導管62a。
Also in FIG. 2, heat exchange tubes 61 whose ends 59 and 60 are rolled up and assembled into a tube bundle are provided, and the fin tubes 5
The ring-shaped conduit 62a leads to the thickened portions 62.63 of 8, which in turn communicate with these portions 62.63.

63aにおいて冷却媒体が供給または導出される。A cooling medium is supplied or withdrawn at 63a.

原料ガス供給導管56より上において、管61により貫
通されて触媒床の底64が延びている。
Above feed gas supply conduit 56 , a bottom 64 of the catalyst bed extends through a tube 61 .

m伏導管63aより上の所に第2の触媒床の底64aが
ある。第2図シこ示す実施例では、底65およびその絶
$1j、966は外被5】およびその絶縁層52と一体
に結合され、メタノールガスを導出する導管67により
貫通され、同様に帽体55およびその絶縁層68も導管
69により貫通されている。
Above the vertical conduit 63a is the bottom 64a of the second catalyst bed. In the embodiment shown in FIG. 2, the bottom 65 and its ends 966 are integrally connected to the jacket 5 and its insulating layer 52 and are pierced by a conduit 67 for conducting methanol gas, which also connects to the cap body. 55 and its insulating layer 68 are also penetrated by a conduit 69.

第1図および第2図による実施例では、管22または6
1は対として反対側にあるひれ70.71をもち、これ
ら管のひれが閉じた流れ空間72を形成し、この空間7
2内の触媒材料を通ってガスが流れるように、配置され
ている。隣接する空間へのガスのW′Mしたがって管2
2.61への不均一な作用は、これによって大幅に回避
される。触媒床の底23,64,64aを一部開くと、
はぼ完全に閉じた空間72により、円筒状外被13.5
7の内部空間をIv次空にする作業を容易に行なうこと
ができる。
In the embodiment according to FIGS. 1 and 2, tube 22 or 6
1 has a pair of opposite fins 70,71, these tube fins forming a closed flow space 72, which space 7
2 is arranged to allow gas to flow through the catalytic material within the catalytic material. W′M of the gas to the adjacent space and therefore the pipe 2
Non-uniform effects on 2.61 are thereby largely avoided. When the bottom 23, 64, 64a of the catalyst bed is partially opened,
Due to the completely closed space 72, the cylindrical jacket 13.5
The work of emptying the internal space of No. 7 to Iv order can be easily carried out.

上下にある2つの融媒床を反応器に収容することはドイ
ツ連邦共和国・特許出願公開第3022815号明罰書
から公知である。この点でそれに向けられてそれに関連
してあげた特徴4よ、本発明の別の特徴と組合わせての
み意味がある。
It is known from DE 30 22 815 A1 to accommodate two melting medium beds one above the other in a reactor. Feature 4, which is directed thereto and listed in connection therewith, has meaning only in combination with other features of the invention.

はぼ円筒状の外被は均等物として円面゛状外被13.5
7と同一視される。
The cylindrical jacket is equivalent to the circular cylindrical jacket 13.5
It is equated with 7.

第4図および第5図によれば、管22ルよ周囲に同じ角
度で分布されて半径方向外方へ向くピン80をもち、こ
れらのピン80は流れ空l¥!j72および触媒床へ突
出し、管の縦方向各こ星状に設けられている。流れ空間
72へ突1川するピンζは異なる高さの所に設けられ、
第5図におし)でピン80′はピン80″より上に、ま
lこピン80” lよピン80”’より上に設けられて
+7’する。
According to FIGS. 4 and 5, the tube 22 has pins 80 distributed at equal angles around its circumference and pointing radially outward, these pins 80 being able to flow through the air. j72 and protrude into the catalyst bed, and are provided in each star shape in the longitudinal direction of the tube. Pins ζ extending into the flow space 72 are provided at different heights,
In FIG. 5), the pin 80' is provided above the pin 80'', and the pin 80''l is provided above the pin 80''' and increases by +7'.

ピン80の長さは、対角線上で隣接する2つの湾例えば
第4図の筐22と22″との間隔の約1/4〜1ハにな
っている。これらのピン番ヨ!まるべく管へ方送まれて
いるか、溶接されてl/)る。
The length of the pin 80 is approximately 1/4 to 1 ha of the distance between two diagonally adjacent bays, for example, the housings 22 and 22'' in FIG. or welded l/).

ピンは正方形断面のピンとしても鋲の形に頭部をもつよ
うに構成することもできる。
The pin can also be configured as a square cross-section pin or with a head in the form of a stud.

【図面の簡単な説明】 第1図は】つの触媒床をもつ′A(発明しこよる反応器
の第1実施例の垂直断面図、第2図・1よ円筒状外被の
円部空間に2つの触媒床を収容する反応器の別の実施例
の垂直断面図、第3図は第1図および第2図による実施
例の触媒床の水平断面Z1第4図は反応器の別の位1[
4−おける水平断面図、第5図シよ第4図のv−■線に
よる断面図である。 ]、51・・・圧力舛被、4,55・・・幌1体、13
157・・・円WJ駅外被、22.61・・・熱交換管
、23.64゜64a・・・触媒床の冗または網、26
・・・触媒床、G・・・ハウジング 第3図 第4図
BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a vertical sectional view of the first embodiment of the reactor according to the invention with two catalyst beds; 3 shows a horizontal section Z1 of the catalyst bed of the embodiment according to FIGS. 1 and 2; FIG. 4 shows another embodiment of the reactor containing two catalyst beds; FIG. Place 1 [
FIG. 5 is a horizontal cross-sectional view taken along the line v--■ in FIG. 4, and FIG. ], 51...Pressure cover, 4,55...1 hood, 13
157... Circle WJ station jacket, 22.61... Heat exchange tube, 23.64゜64a... Catalyst bed redundancy or net, 26
...Catalyst bed, G...Housing Fig. 3 Fig. 4

Claims (1)

【特許請求の範囲】 1 ハウジング内部にある触媒床を貫通する熱交換管を
もつ円筒状ハウジングと、反応器下部にあって触媒床を
支えるガス透過底またCt網とを有するものにおいて、
ハウジング(G)が上にある帽体(4,55)により閉
鎖され、ノAウジング(G)内、にあって触媒床(26
)を包囲する円筒状外被(13,57)が、一体(4,
55)を取外して触媒床(26)と共に反応器の縦方向
にそのハウジング(G)から取出し可能であることを特
徴とする、メタノールの製造用直立反応器。 2 円筒状外被(13,57)がひれ付き管(1,2,
58)から形成されていることを特徴とする特許請求の
範囲第1項に記載の反応器。 3 円筒状外被(13,57)のひれ付き管(12,5
8)の上部(14,62)および下部(15,63)へ
、円筒状外被(13,5,7)の内部空間を均一に貫通
して反応器縦軸−に対して平行に延びる複数の熱交換管
(22,61)の曲げられた端!(2o+21および5
9.60)が通じていることを特徴とする特許請求の範
囲第2項に記載の反応器。 4 円筒状外被(t3+57’)を形成するひれ付き管
(第2,58)が、反応器下部で環状導管(+6+63
a)へ通じ、触媒床を支えるガス透過底または網(23
,6411)が、環状導管(16,63a)の高さの所
で、との環状導管(16+ 63a )にまたはそのす
ぐ上で円筒状外被(13,57)の管部分(15,63
)に取付けられていることを特徴とする特許請求の範囲
第2項または第3項に記載の反応器。 5 円筒状外被(+3.57)の内部空間を反応器縦軸
線に対して平行に貫通する熱交換管(22,61)がひ
れ(70,71)を備えて、これらの熱交換管(22,
61)と隣接する熱交換管のひれ(7017i)とが、
触媒材料を満たされる規則正しい幾何学的断面の閉じた
流れ空間(72)を形成していることを特徴とする特許
請求の範囲第2項ないし第4項のいずれか1つに記載の
反応器。 6 円筒状外被(57)の内部空間が上下に設けられる
2つの触媒床を収容し、ガス供給導管(56)が上部触
媒床より下および下部触媒床より上で反応器へ通じてい
ることを特徴とする特許請求の範囲第1項ないし第5項
のいずれか1つに記載の反応器。 7 反応器へのガス供給導管(56)より上において触
媒床の底まなは網(64)が、熱交換管(61)の貫通
する円筒状外被(57)の断面にわたって延びているこ
とを特徴とする特許請求の範囲第6項に記載の反応器。 8 下にある反応器の底(65)と上にある反応器の副
体(55)がそれぞれメタノールガス用のガス取出し導
管(67,69)をもっていることを特徴とする特許請
求の範囲第6項に記載の反応器。 9 s体(4,)をハウジングCG)の中間部分(1)
と結合するフランジ(2,5)の分雛面までまたはその
下まで充填触・媒が達していることを特徴とする特許請
求の範囲第1項または第6項めいずれか1つに記載の反
応器。 10 ひれ(70,71)により閉じられかつ触媒材料
を満たされる規則正しい幾何学的断面の流れ空間(72
)を形成する熱交換管(22)が、流れ空間(72)へ
対称に突出する半径方向ピン(8o)をもち、1つの流
れ空間(72)のピン(8o)が異なる高さで熱交換管
(22)に設けられていることを特徴とする特許請求の
範囲第5項に記載の反応器。 】1 ピン(80)が対角線上で@接する2つの熱交換
管(22,22”)の間隔の約1/4〜I73の長さを
もっていることを特徴とする特許請求の範囲第10項に
記載の反応器。 I2.ピン(8o)が管壁へ打込まれていることを特徴
とする特許請求の範囲第10項または第11項に記載の
反応器。 】3 熱交換管(22)のひれ(70,7])が対をな
して管に溶援されていることを特徴とする特許請求の範
囲第I0項に記載の反応器。
[Claims] 1. A cylindrical housing having a heat exchange tube that penetrates a catalyst bed inside the housing, and a gas permeable bottom or Ct net that supports the catalyst bed at the bottom of the reactor,
The housing (G) is closed by an overlying cap (4, 55) and is located within the housing (G) and contains a catalyst bed (26).
A cylindrical jacket (13, 57) surrounding the integral parts (4, 57)
55) An upright reactor for the production of methanol, characterized in that it can be removed and removed together with the catalyst bed (26) from its housing (G) in the longitudinal direction of the reactor. 2 The cylindrical jacket (13, 57) is attached to the finned tube (1, 2,
58) The reactor according to claim 1, characterized in that it is formed from: 3 Fin tube (12,5) with cylindrical jacket (13,57)
8) to the upper part (14, 62) and lower part (15, 63) of the cylindrical jacket (13, 5, 7), extending parallel to the longitudinal axis of the reactor through the interior space of the cylindrical jacket (13, 5, 7). The bent end of the heat exchange tube (22, 61)! (2o+21 and 5
9.60) is in communication with the reactor according to claim 2. 4 The fin tube (No. 2, 58) forming the cylindrical jacket (t3+57') connects to the annular conduit (+6+63) at the bottom of the reactor.
a) gas permeable bottom or screen (23
, 6411) of the cylindrical jacket (13, 57) at the level of the annular conduit (16, 63a) and directly above the annular conduit (16+ 63a).
) The reactor according to claim 2 or 3, characterized in that it is attached to a reactor. 5 Heat exchange tubes (22, 61) passing through the internal space of the cylindrical jacket (+3.57) parallel to the longitudinal axis of the reactor are equipped with fins (70, 71) and these heat exchange tubes ( 22,
61) and the adjacent fin (7017i) of the heat exchange tube,
5. Reactor according to any one of claims 2 to 4, characterized in that it forms a closed flow space (72) of regular geometric cross section filled with catalyst material. 6. The internal space of the cylindrical envelope (57) accommodates two catalyst beds arranged one above the other, and the gas supply conduit (56) leads to the reactor below the upper catalyst bed and above the lower catalyst bed. A reactor according to any one of claims 1 to 5, characterized in that: 7. Note that above the gas supply conduit (56) to the reactor, the bottom manifold (64) of the catalyst bed extends over the cross section of the cylindrical jacket (57) through which the heat exchange tube (61) passes. A reactor according to claim 6, characterized in: 8. Claim 6, characterized in that the lower reactor bottom (65) and the upper reactor side body (55) each have a gas removal conduit (67, 69) for methanol gas. Reactor as described in Section. 9 s body (4,) to the middle part (1) of the housing CG)
Claims 1 or 6, characterized in that the packed catalyst reaches up to or below the splitting surface of the flanges (2, 5) that are connected to the flanges (2, 5). reactor. 10 flow spaces (72) of regular geometrical cross-section closed by fins (70, 71) and filled with catalyst material;
) with radial pins (8o) projecting symmetrically into the flow space (72), the pins (8o) of one flow space (72) exchanging heat at different heights. 6. Reactor according to claim 5, characterized in that it is provided in a tube (22). 10. Claim 10, characterized in that the pin (80) has a length of approximately 1/4 to I73 of the distance between the two diagonally contacting heat exchange tubes (22, 22"). Reactor according to claim 10 or claim 11, characterized in that the pin (8o) is driven into the tube wall.]3 Heat exchange tube (22) 10. Reactor according to claim 10, characterized in that the fins (70, 7]) are fused into the tube in pairs.
JP17422284A 1983-09-06 1984-08-23 Vertical reactor for methanol manufacture Granted JPS6061544A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19833332049 DE3332049A1 (en) 1983-09-06 1983-09-06 Upright reactor for methanol production
DE3332049.7 1983-09-06
DE3344423.4 1983-12-08

Publications (2)

Publication Number Publication Date
JPS6061544A true JPS6061544A (en) 1985-04-09
JPH0437809B2 JPH0437809B2 (en) 1992-06-22

Family

ID=6208321

Family Applications (1)

Application Number Title Priority Date Filing Date
JP17422284A Granted JPS6061544A (en) 1983-09-06 1984-08-23 Vertical reactor for methanol manufacture

Country Status (2)

Country Link
JP (1) JPS6061544A (en)
DE (1) DE3332049A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2010013422A (en) * 2008-07-07 2010-01-21 Takuma Co Ltd Methanol synthesis reactor and methanol synthesis method
CN109395670A (en) * 2018-09-30 2019-03-01 中石化宁波工程有限公司 The temperature shift reactions device such as alternating temperature

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3441917A1 (en) * 1983-09-06 1986-05-28 MAN Gutehoffnungshütte GmbH, 4200 Oberhausen Vertical reactor for producing methanol
US4743432A (en) * 1984-11-16 1988-05-10 M.A.N. Maschinenfabrik Augsburg-Nurnberg Vertical reactor for the generation of methanol
DE3605792A1 (en) * 1985-09-27 1987-04-02 Gutehoffnungshuette Man STANDING REACTOR FOR CATALYTIC EXOTHERM AND ENDOTHERM REACTIONS, ESPECIALLY FOR THE PRODUCTION OF METHANOL, AMMONIA, SYNTHESIS GAS AND HIGHER ALCOHOLS
DE3708230A1 (en) * 1987-03-13 1988-09-22 Uhde Gmbh Apparatus for carrying out catalytic reactions with gaseous fluids

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1803306A (en) * 1927-01-08 1931-04-28 Commercial Solvents Corp Catalytic apparatus
DE3007203A1 (en) * 1980-02-26 1981-09-10 Linde Ag, 6200 Wiesbaden Methanol synthesis reactor - with catalyst packing contg. coolant pipes aligned parallel with flow of synthesis gas to minimise drop in gas pressure

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2010013422A (en) * 2008-07-07 2010-01-21 Takuma Co Ltd Methanol synthesis reactor and methanol synthesis method
CN109395670A (en) * 2018-09-30 2019-03-01 中石化宁波工程有限公司 The temperature shift reactions device such as alternating temperature
CN109395670B (en) * 2018-09-30 2022-04-12 中石化宁波工程有限公司 Temperature-changing isothermal transformation reaction device

Also Published As

Publication number Publication date
DE3332049A1 (en) 1985-03-21
JPH0437809B2 (en) 1992-06-22
DE3332049C2 (en) 1987-10-22

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