JPS60137431A - Apparatus for reaction or adsorption due to radius flow - Google Patents

Apparatus for reaction or adsorption due to radius flow

Info

Publication number
JPS60137431A
JPS60137431A JP58247925A JP24792583A JPS60137431A JP S60137431 A JPS60137431 A JP S60137431A JP 58247925 A JP58247925 A JP 58247925A JP 24792583 A JP24792583 A JP 24792583A JP S60137431 A JPS60137431 A JP S60137431A
Authority
JP
Japan
Prior art keywords
catalyst
reaction
adsorption
adsorbent
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.)
Granted
Application number
JP58247925A
Other languages
Japanese (ja)
Other versions
JPH0135690B2 (en
Inventor
Morihisa Hidaki
肥田木　盛久
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.)
Toyo Engineering Corp
Original Assignee
Toyo Engineering Corp
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 Toyo Engineering Corp filed Critical Toyo Engineering Corp
Priority to JP58247925A priority Critical patent/JPS60137431A/en
Publication of JPS60137431A publication Critical patent/JPS60137431A/en
Publication of JPH0135690B2 publication Critical patent/JPH0135690B2/ja
Granted legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical 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
    • B01J8/0207—Chemical 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 flow within the bed being predominantly horizontal

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  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

PURPOSE:To make pressure drop small by providing uniformly many perforated pipes whose upper ends are opened to the space above a layer of catalyst or adsorbent on the inner wall of adsorption vessel. CONSTITUTION:Gaseous raw material is flowed in from an inlet 9 and most parts of said raw material are introduced into perforated pipes 4 from these upper parts and flowed out from the holes of the pipes and passed through a catalyst layer to enter an inside basket 5 and flowed out from a gas outlet 10. The perforated pipes 4 are buried in the range up to the under part from the upper part of the catalyst layer and opened to the space above mentioned layer and also provided along the inner wall of adsorption vessel uniformly and vertically. In this way, the cost reduction is made possible.

Description

【発明の詳細な説明】 この発明は固体触媒あるいは吸着剤を使用し、ガス状転
化反応または吸着を起させる反応または吸着装置の改良
に関する。DETAILED DESCRIPTION OF THE INVENTION This invention relates to an improvement in a reaction or adsorption device that uses a solid catalyst or adsorbent to cause a gaseous conversion reaction or adsorption.

なおこの明細書においては、ガス状原料と接触する゛触
媒あるいは吸着剤゛′を単に“触媒″、生起せしめられ
た゛′反応または吸着″を単に“反応″、および゛多孔
管または多孔板または高空間率充填物″を単に゛多孔管
″とこのあと呼ぶことにする。（吸着では通常、吸着剤
と被吸着物質の間に化学反応は起らないのであるが。） 竪型円筒容器に触媒を充填した反応装置の形式としては
、ガスの流れ方向により、軸流と半径流に大別される。In this specification, a ``catalyst or adsorbent'' that contacts a gaseous raw material is simply referred to as a ``catalyst'', a ``reaction or adsorption'' that occurs is simply referred to as a ``reaction'', and a ``perforated tube, perforated plate, or high From now on, we will simply refer to the ``porous tube'' as the ``porous tube.'' (Normally, in adsorption, no chemical reaction occurs between the adsorbent and the adsorbed substance.) A catalyst is placed in a vertical cylindrical container. The types of reactors filled with gas are broadly classified into axial flow and radial flow depending on the direction of gas flow.

軸流は棚の上に触媒を充填した最も普通に使用されてい
るものであり、ガスは中心軸方向（下向きの場合が多い
）に流れる。第１図（ａ　）に示す。Axial flow is the most commonly used with catalyst packed on shelves, where the gas flows in a central axial direction (often downward). It is shown in FIG. 1(a).

半径流は容器の中心軸と同軸に設けられた内側と外側の
バスケットの間を半径方向に流れる。触媒層の上下は仕
切り板によって閉ぢられているのが普通である一部１図
（ｂ）に示す。中には上部の仕切り板の一部を省略して
、ガスの一部分を軸流で流す方式のものもある。第１図
（Ｃ）に示ず。Radial flow flows radially between inner and outer baskets that are coaxial with the central axis of the container. The top and bottom of the catalyst layer are usually closed by partition plates, as shown in Figure 1(b). Some models omit part of the upper partition plate and allow part of the gas to flow axially. Not shown in FIG. 1(C).

軸流は構造簡単であるが、ガス流邑が多くなり、また触
媒量が多くなると圧力降下の上昇を防ぐため水平断面を
大きくせねばならず、径の大きい容器が必要となる。Axial flow has a simple structure, but as the number of gas streams increases and the amount of catalyst increases, the horizontal cross section must be increased to prevent pressure drop from increasing, and a container with a large diameter is required.

これに比し半径流では通路断面積を大きくとれ、また通
路長さが短くなるので、圧力降下が非常に低下する。ガ
ス流量が大きく、触媒量が多い場合は最も好ましい装置
の形式である。In contrast, with radial flow, the cross-sectional area of the passage can be increased and the length of the passage can be shortened, resulting in a very low pressure drop. This is the most preferred type of device when the gas flow rate is large and the amount of catalyst is large.

しかしながら内外のバスケットおよび上下の仕切り板等
構造がやや複雑になり、コストが高くなる欠点−がある
。特に反応熱などにより、運転温度が高くなったり、ま
た温度変動のあるものなどでは、触媒層の伸縮に対応す
るためバスケットの強度を増す必要があり、かなりのコ
スト高を免かれない。However, the structure of the inner and outer baskets, the upper and lower partition plates, etc. is somewhat complicated, and the cost is high. Particularly in cases where the operating temperature is high due to reaction heat, or where there are temperature fluctuations, it is necessary to increase the strength of the basket to accommodate the expansion and contraction of the catalyst layer, resulting in a considerable increase in cost.

第１図（、Ｃ）のものは、上部仕切り板の一部を省略し
て流路面積をさらに大きくし、かつコスト減をはかった
ものであるが、しかしくｂ）との差はそれ程大きくはな
い。The one in Figure 1 (, C) omitted part of the upper partition plate to further increase the flow path area and reduce costs, but the difference from b) is not that large. There isn't.

この発明は半径流の反応装置において、半径流の最大の
特徴である圧力降下が小さいという特徴を保持しつつ、
コストの安い装置を提供するものである。This invention is a radial flow reactor that maintains the most important feature of radial flow, which is low pressure drop.
This provides a low-cost device.

この発明の基本的な考え方は、コストの中で大きい割合
を占める外側のバスケットの代りに、多孔管を容器の内
壁上に等間隔に鉛直に設けることである。The basic idea of the invention is to provide perforated tubes vertically and equidistantly on the inner wall of the container, instead of an outer basket which accounts for a large proportion of the cost.

この多孔管の上端は触媒層の上部空間に開口しており、
下端は触媒層の下端に達し、周囲には触媒が充填されて
いる。ガスはこの上部開口部から流入し、多孔管の孔か
ら触媒層内に流出する。多孔管の寸法および孔の径と数
を適当に選択することにより、ガスを略均等に触媒層を
半径方向に流動させることができる。また多孔管の数は
、全体のガス量、触媒層の寸法等を考慮の１均等に流れ
るように設計できる。The upper end of this porous tube opens into the upper space of the catalyst layer,
The lower end reaches the lower end of the catalyst layer, and the surrounding area is filled with catalyst. Gas enters through this upper opening and flows out through the pores of the perforated tube into the catalyst layer. By appropriately selecting the dimensions of the porous tube and the diameter and number of holes, it is possible to cause the gas to flow approximately uniformly in the radial direction of the catalyst layer. Further, the number of porous tubes can be designed so that the gas flows evenly, taking into account the total amount of gas, the dimensions of the catalyst layer, etc.

この多孔管の孔の部分、および内側バスケットの流入部
分に多少抵抗をつけることにより、流最が均一になるよ
うに調節することができる。なおこの多孔管の外側は触
媒が孔を詰めたりしないように、金網等で巻くのが望ま
しい。By adding some resistance to the hole portion of the porous tube and the inflow portion of the inner basket, the flow can be adjusted to be uniform. Note that it is desirable to wrap the outside of this porous tube with a wire mesh or the like to prevent the catalyst from clogging the pores.

また多孔管は触媒層に深く埋っているので、特別に固定
する必要はないのであるが、据付時のこともあるので、
内壁から上下を保持するようにするのがよい。多孔管が
フリーに伸び得るように保持されるのが望ましい。Also, since the porous tube is deeply buried in the catalyst layer, there is no need to specially fix it, but it may be necessary to fix it during installation.
It is best to hold the top and bottom from the inner wall. Preferably, the perforated tube is held so that it can extend freely.

多孔管は単に埋っているだけで、荷重等はとんど受けな
いので特別な規格、材料のものは必要とせず、通常の鋼
管に孔をあけたものでよい。仮に水素脆化等によってク
ラック等を生じたとしても、特に問題とするような事態
にはならない。Since perforated pipes are simply buried and do not receive much load, they do not require special specifications or materials; they can be ordinary steel pipes with holes drilled in them. Even if cracks or the like were to occur due to hydrogen embrittlement or the like, this would not pose any particular problem.

この多孔管としては円形管の使用が通常であるが、それ
以外の異形管でも使用できる。例を第２図に示す。Although a circular tube is normally used as this perforated tube, other irregularly shaped tubes can also be used. An example is shown in FIG.

（ａ）は普通の円形管、（ｂ）、（ｃ）は型鋼を加工し
たもの、（ｄ　＞は半割円形管を加工したもの、（ｅ　
）は円形管に突起パイプをつけ、ガスの分散を良くした
ものである。(a) is an ordinary circular tube, (b) and (c) are made from shaped steel, (d > is made from a half-split circular tube, (e
) is a circular tube with protruding pipes to improve gas dispersion.

またこの″多孔管″は周囲が閉じている、所謂管″でな
くてもよい。即ち多孔板あるいは高空間率充填物であっ
ても良い。第２図（１、（０）に示すように反応容器の
器壁との間に原料ガスが流入する空間を作るものであれ
ば良いのである。図によってわかるように、この多孔板
を反応容器の壁面に密接に取りつけ、触媒を充填すれば
この多孔板は器壁に押しつけられ、好適なガス通路とな
るのである。Moreover, this "perforated pipe" does not have to be a so-called pipe with a closed periphery.In other words, it may be a perforated plate or a high porosity filling.As shown in Fig. 2 (1, (0)) Any device that creates a space for the raw material gas to flow in between the wall of the reaction vessel and the wall of the reaction vessel is fine. The perforated plate is pressed against the vessel wall and provides a suitable gas passage.

第２図（ｂ）、（Ｃ）、（’ｄ　）においても、背中の
蓋は触媒がこの中に入らぬようにできれば、必ずしも必
要ではない。In FIGS. 2(b), (C), and ('d), the back cover is not necessarily necessary as long as the catalyst can be prevented from entering the back cover.

あるいは高空間率充填物、例えばラツシピリングのよう
な充填物を器壁にそって充填してもよい。規則正しく充
填することにより、好適なガスの通路となる。Alternatively, a high porosity packing, such as a lacquer ring, may be filled along the vessel wall. Regular filling provides a suitable gas passage.

このようにこの“多孔管″は種々の変形が可能である。In this way, this "perforated tube" can be modified in various ways.

コストのかかる外側バスケットの代りに、このように簡
単でコストの安い多孔管を使用することによって、半径
流の長所を全く損なうことなく、コストの安い反応装置
が実現できるのである。By using such a simple and inexpensive perforated tube instead of a costly outer basket, a less expensive reactor can be realized without sacrificing any of the advantages of radial flow.

なおガスの流れは外側から内側へでも、その反対に内側
から外側へでも、どちらでも可能である。また場合によ
っては、例えば吸着剤の場合、吸着時には外から内へ、
脱着時には内から外へ、あるいはこの逆に、ガスの流れ
の方向を変えるような場合でも使用可能である。Note that the gas can flow either from the outside to the inside or vice versa. In some cases, for example, in the case of adsorbents, when adsorbing, from the outside to the inside,
It can also be used in cases where the direction of gas flow is changed from inside to outside or vice versa during desorption.

次に図面により説明する。Next, it will be explained with reference to the drawings.

第３図はこの発明を適用した１例である。FIG. 3 shows an example to which this invention is applied.

図において、１１反応容器、２．上部鏡板、３．下部鏡
板、４．多孔管、５．内側バスケット、６．触媒、７．
断熱剤である 原料ガスは入口９から流入し、大部分は多孔管４に上か
ら入り、管の孔から流出、触媒層を通過して内側バスケ
ット５に入り、ガス出口１０から流出する。In the figure, 11 reaction vessels, 2. Upper mirror plate, 3. Lower mirror plate, 4. Porous tube, 5. inner basket, 6. catalyst, 7.
The raw material gas, which is a heat insulating agent, flows in from the inlet 9, most of which enters the porous tube 4 from above, flows out through the holes in the tube, passes through the catalyst layer, enters the inner basket 5, and flows out from the gas outlet 10.

多孔管は触媒層の上から下に至るまで埋っており、触媒
層の上部空間に開口している。そして反応容器の内壁に
そって等間隔に鉛直に置かれている。触媒層を通過する
ガス量はできる限り均等で偏りがないようにしなければ
ならない。このためには各多孔管から流出するガス量が
等しく、また１本の多孔管をとっても、その管の部位に
よって偏りがないことが望ましい。内側バスケットにつ
いても同様のことが言える。The porous tube is buried from the top to the bottom of the catalyst layer and opens into the space above the catalyst layer. They are placed vertically at equal intervals along the inner wall of the reaction vessel. The amount of gas passing through the catalyst layer must be as uniform and unbiased as possible. For this purpose, it is desirable that the amount of gas flowing out from each porous tube be equal, and even within a single porous tube, there should be no bias depending on the location of the tube. The same can be said for the inner basket.

このように流量を均一に偏りをなくする、最も簡単な方
法は、各部の寸法を同じ寸法とし、かつこの多孔管およ
び内側バスケットの通過抵抗を、触媒層の通過抵抗より
太き目に取ることである。特に内側バスケットに流入す
るガス量の分布を充分にコントロールすることが重要で
ある。前者と後者の比率が大きくなればなる程その均一
性はよくなる。しかしあまり大きくすると、その割には
均一性が良くならず、また半径流反応装置の利点である
圧力降下が小さいという利点も失はれるので、適当な値
になるよう設計するのが重要である。The easiest way to make the flow rate uniform and unbalanced is to make the dimensions of each part the same, and to make the passage resistance of the perforated tube and inner basket larger than the passage resistance of the catalyst layer. It is. In particular, it is important to sufficiently control the distribution of the amount of gas flowing into the inner basket. The greater the ratio between the former and the latter, the better the uniformity. However, if it is made too large, the uniformity will not be as good and the advantage of the radial flow reactor, which is the small pressure drop, will also be lost, so it is important to design it to an appropriate value. .

第３図におけるこの装置のもう１つの特徴は、触媒の上
部に仕切り板がなく、内側バスケットが触媒層内に埋っ
ていることである。このような反応の場合、ガスの流れ
る方向は特に問題ではなく、触媒層をなるべく均一に流
れさえすればよいわけである。Another feature of this device in FIG. 3 is that there is no partition plate on top of the catalyst, and the inner basket is buried within the catalyst bed. In the case of such a reaction, the direction in which the gas flows does not particularly matter, as long as it flows as uniformly as possible through the catalyst layer.

従って第３図のような場合、上部に仕切り板をつけるこ
とは意味がないことである。ガスは触媒層を通過して、
内側バスケットに流入しさえすれば良いのである。内側
バスケットの頂部を触媒層内に埋めておき、その側面の
全部または側面および頂部がガス通過可能なようにして
おけば、この頂部の上にある触媒も同じく触媒層として
働く。ここを通過するガス量はその部分のスペースベロ
シティが、全体のスペースベロシティと同じになるよう
に定めればよい。Therefore, in the case shown in Figure 3, it is meaningless to attach a partition plate to the top. The gas passes through the catalyst layer,
All that is required is for it to flow into the inner basket. If the top of the inner basket is buried in the catalyst layer and all or the sides and the top are gas permeable, the catalyst above the top also acts as a catalyst layer. The amount of gas passing through this area may be determined so that the space velocity of that part is the same as the space velocity of the whole.

このような条件から実際の寸法は決められるわけである
が、上部仕切り板および内側バスケットの上部が不要と
なり、それだけコストは低減する。Although the actual dimensions are determined based on these conditions, the upper partition plate and the upper part of the inner basket are no longer necessary, and the cost is reduced accordingly.

このような場合、触媒層の上部を水平に充填すると、上
部外側の触媒の部分は、内側バスケット頂部からの距離
が大きくなるので、ガスが通過しにくくなる。つまりこ
の部分はデッドスペースとなり、反応にほとんど無関係
となる。このような無効な部分に貴重な触媒を積んでお
くのは無駄なことである。In such a case, if the upper part of the catalyst layer is filled horizontally, the part of the catalyst on the outside of the upper part has a greater distance from the top of the inner basket, making it difficult for gas to pass through. In other words, this part becomes a dead space and is almost unrelated to the reaction. It is wasteful to store valuable catalysts in such ineffective areas.

この無駄をなくするには、内側バスケット頂部からの距
離がほぼ等しいように、上部を球形にすればよい。こう
することにより、球形の面から流入し、触媒層を通過し
、内側バスケットに流入するガスの流れは略均−となり
、触媒はすべて有効に働くことになる。To eliminate this waste, the upper part can be made spherical so that the distance from the top of the inner basket is approximately equal. By doing so, the flow of gas flowing from the spherical surface, passing through the catalyst layer, and flowing into the inner basket is approximately equal, and all of the catalysts work effectively.

しかし上面をこのように球形のままにしておくのは具合
が悪い。長期の運転では山が崩れてしまう危険が強いか
らである。これを防止するためには、球形面とその頂部
を通る水平面との間の空間に、非触媒あるいは非吸着質
充填物８を充填しておけばよい。However, it would be inconvenient to leave the top surface spherical like this. This is because there is a high risk of the mountain collapsing during long-term driving. In order to prevent this, a non-catalytic or non-adsorptive filler 8 may be filled in the space between the spherical surface and the horizontal plane passing through the top of the spherical surface.

例えばアルミナボールあるいは磁製ラツシピリングのよ
うなものが適当である。ガスの通過が容易な充填物を使
用するのが望ましい。このような充填物で触媒層表面を
覆うことは、適当な粒子押えともなり、特にガスが下方
から上方に流れる時有効である。For example, alumina balls or porcelain lash pillings are suitable. It is desirable to use a filling through which gas can easily pass. Covering the surface of the catalyst layer with such a filler also serves as a suitable particle suppressor, and is particularly effective when gas flows from the bottom to the top.

なお内側バスケットの上面は、球形ないし半楕円形にす
るのがガスの流れが均一となり、強度の面からも有利で
あり、望ましいことである。It is preferable that the upper surface of the inner basket be spherical or semi-elliptical, as this will ensure uniform gas flow and is advantageous in terms of strength.

第３図に示した装置の、さらにもう１つの特徴は、下部
の触媒棚あるいは仕切り板がないことである。Yet another feature of the apparatus shown in FIG. 3 is the absence of a lower catalyst shelf or partition.

軸流の反応装置では粒子を支持棚の上に充填するのが通
常のやり方である。半径流の装置でも支持棚あるいは仕
切り板をとりつけ、この上に触媒を充填するのが通常の
やり方である。第１図（ｂ’）、（Ｃ）参照。In axial flow reactors it is common practice to pack the particles onto support shelves. Even in radial flow devices, it is common practice to install a support shelf or partition plate on which the catalyst is packed. See FIGS. 1(b') and (C).

触媒支持棚あるいは仕切り板は触媒の荷重のみならず、
ガスが上部から下方に流れる場合は、圧力降下に相当す
る分の荷重も受けるので、かなりの荷重となり、相当の
コストとなる。半径流反応装置の場合は、触媒を下部鏡
板の上に直接充填するようにすればここのような棚ある
いは板は不要となる。ガスの流れは多孔管、内側バスケ
ット、下部鏡板の形状等について充分注意深く設計をす
れば問題ないようにできる。ガスの流れの点からは下部
鏡板は半球より半楕円あるいは皿型の鏡板の方が適して
いる。The catalyst support shelf or partition plate not only supports the load of the catalyst, but also
When gas flows downward from the top, it also receives a load corresponding to the pressure drop, resulting in a considerable load and considerable cost. In the case of a radial flow reactor, if the catalyst is packed directly onto the lower end plate, such a shelf or plate is not required. Problems with gas flow can be avoided by carefully designing the shape of the perforated pipe, inner basket, lower head plate, etc. From the point of view of gas flow, a semi-elliptical or dish-shaped lower end plate is more suitable than a hemispherical end plate.

発熱反応の場合は、温度によっては下部鏡板に断熱材を
敷くのが望ましい。例えば原料ガスが外側から内側へ流
れる場合、鏡板は中心に近い程温度の高いガスと接触す
るようになり、鏡板の機械的強度を損い、あるいは材料
の損傷を招くことも起り得る。In the case of an exothermic reaction, depending on the temperature, it is desirable to place a heat insulating material on the lower head plate. For example, when the raw material gas flows from the outside to the inside, the closer the end plate is to the center, the higher the temperature of the gas comes into contact with the end plate, which may impair the mechanical strength of the end plate or cause damage to the material.

このような場合、下部鏡板の上に断熱材７を敷いて、鏡
板の温度が上り過ぎるのを防止できる。In such a case, a heat insulating material 7 can be placed on the lower end plate to prevent the temperature of the end plate from rising too much.

このための断熱材としては板状の無機断熱材が適当であ
る。これを鏡板の上に敷き、この上に断熱煉瓦等を敷き
つめておけばよい。As a heat insulating material for this purpose, a plate-shaped inorganic heat insulating material is suitable. All you have to do is spread this on top of the mirror board and then cover it with insulation bricks, etc.

温度が更に高くなれば本格的なライニングをする必要が
あるが、その場合は断熱材が鋼材に密着するので、鋼材
の表面を点検することが普通はできない。If the temperature rises even higher, full-scale lining will be necessary, but in that case the insulation adheres closely to the steel, so it is usually not possible to inspect the surface of the steel.

この発明の断熱法は鏡板に断熱材を置くだけであるので
、点検が必要な場合は断熱材を外して容易に点検できる
。Since the heat insulation method of this invention simply places a heat insulating material on the mirror plate, if inspection is required, the heat insulating material can be removed and inspected easily.

反応温度がそれ程高くない場合は、鏡板の保護のための
断熱にはこれで充分であり、鏡板材料の強度は容器の胴
体部分と同じと見ることができる。なおこの場合、鏡板
の外面は鏡板の温度をなるべく低く保つため、保温しな
い方がよい。If the reaction temperature is not very high, this is sufficient for heat insulation to protect the head plate, and the strength of the head plate material can be considered to be the same as that of the body of the container. In this case, it is better not to keep the outer surface of the end plate warm in order to keep the temperature of the end plate as low as possible.

ガスの出口付近は温度の高い反応ガスに接触し、局部的
に温度が上ることがあるので注意が肝要である。断熱を
施すとか、材質を変えるとかの対策が必要な場合がある
。It is important to be careful as the area near the gas outlet will come into contact with the high temperature reaction gas and the temperature may rise locally. Measures such as providing insulation or changing the material may be necessary.

以上述べたように、第３図は特許請求の範囲第１項から
第４項までの要件をすべて含んでいる。第１項のみの場
合は第１図（ｂ）において外側バスケットを多孔管に代
えただけであるので、図面には示してない。As described above, FIG. 3 includes all the requirements of claims 1 to 4. In the case of only item 1, the outer basket in FIG. 1(b) is simply replaced with a perforated pipe, and is therefore not shown in the drawing.

冷却熱媒体が内部を流通する冷却管で、触媒層を冷却す
るのはよく行われている方法である。吸着装置の場合は
ほとんど行われていないが、反応熱の大きい反応装置に
は適用される場合が多い。It is a common method to cool the catalyst layer using a cooling pipe through which a cooling heat medium flows. Although it is rarely used in adsorption equipment, it is often applied to reaction equipment that generates a large amount of heat of reaction.

この発明による装置にも、この冷却管を装備することが
可能である。熱媒体が水で、冷却管でボイラーを形成し
ている場合が多い。ガスの流れおよび温度分布が均一に
なるために、冷却管は触媒層に垂直に、容器の中心軸と
同じ中心を持つ１または複数の同心円上に、それぞれ等
間隔に配列されていることが望ましい。The device according to the invention can also be equipped with this cooling pipe. In many cases, the heat medium is water and cooling tubes form a boiler. In order to make the gas flow and temperature distribution uniform, it is desirable that the cooling pipes be arranged perpendicular to the catalyst layer and at equal intervals on one or more concentric circles having the same center as the central axis of the container. .

この冷却管の装着方法は、この種の反応器に対する装着
法と同様であるので、詳細な説明は省略するが、一般的
に使用できるものとして、バヨネット型のボイラーを備
えたものがある。The method of installing this cooling pipe is the same as the method of installing this type of reactor, so a detailed explanation will be omitted, but one that can be generally used is one equipped with a bayonet type boiler.

次にこの発明を適用した実施例を紹介する。Next, an example to which this invention is applied will be introduced.

−酸化炭素高温転化反応器 原料ガス　水素、窒素、−酸化巖素、水蒸気混合ガス 入口温度　３７０℃ 出口温度　４４０℃ 圧力　３０ｋａ／ｃｗｌＱ 第３図に示したものがそのまま本例にあてはまる。-Carbon oxide high temperature conversion reactor Raw material gas Hydrogen, nitrogen, sulfur oxide, water vapor mixed gas Inlet temperature 370℃ Outlet temperature 440℃ Pressure 30ka/cwlQ What is shown in FIG. 3 applies directly to this example.

反応によって温度が高くなり、鏡板材料の強度および水
素脆化が問題となる。そのため下部鏡板の上に断熱板を
置き、断熱しである。The reaction raises the temperature, which poses problems in terms of the strength of the end plate material and hydrogen embrittlement. Therefore, a heat insulating plate is placed on top of the lower mirror plate to insulate it.

アンモニア合成装置 これは中間熱交換冷却式断熱反応装置で触媒層が３層の
ものである。触媒層は半径流で、ガスは外側から内側に
流れる。この触媒層に本発明が適用されている。Ammonia synthesis device This is an intermediate heat exchange cooling type adiabatic reaction device with three catalyst layers. The catalyst bed has a radial flow, with gas flowing from the outside to the inside. The present invention is applied to this catalyst layer.

原料ガスは入口９から入り、熱交換器１１のチューブ側
で加熱され、大部分のガスは多孔管４を経テ外側から、
一部分のガスは上部から触媒層に流入し、アンモニア合
成反応を起す。ガスは次に熱交換器のシェル側に流入し
、ここで冷却されたガスは、次の触媒層で更に反応を起
し、順次触媒層および熱交換器のシェル側を通った後、
最後に熱交換して出口１０から流出する。The raw material gas enters from the inlet 9 and is heated on the tube side of the heat exchanger 11, and most of the gas passes through the perforated tube 4 from the outside.
A portion of the gas flows into the catalyst layer from the top and causes an ammonia synthesis reaction. The gas then flows into the shell side of the heat exchanger, where the cooled gas undergoes further reaction in the next catalyst layer, and after successively passing through the catalyst layer and the shell side of the heat exchanger.
Finally, it exchanges heat and flows out from the outlet 10.

触媒層の外側バスケットの代りに多孔管が使用されてい
る。また触媒層上面には仕切り板がなく、触媒は球形に
山盛に充填されていて、非触媒質の充填物が上面が平に
なるように充填されている。最後の触媒層は鏡板の上に
置かれた断熱材の上に充填されている。A perforated tube is used instead of the outer basket of the catalyst layer. Further, there is no partition plate on the upper surface of the catalyst layer, and the catalyst is packed in spherical heaps, and the non-catalytic filler is packed so that the upper surface is flat. The final catalyst layer is packed onto a heat insulating material placed on top of the end plate.

触媒層入口のガス温度は３６０〜３８０℃、触媒層出口
温度は４６０〜４００℃程度である。The gas temperature at the inlet of the catalyst layer is about 360-380°C, and the temperature at the outlet of the catalyst layer is about 460-400°C.

本発明を適用することにより、多段半径流反応装置のコ
スト低減が可能となる。また下部の断熱材の効果と相俟
って、容器を高温における強度によって設計する、所謂
“小ツトウォールデザイン″が可能となる。By applying the present invention, it is possible to reduce the cost of a multistage radial flow reactor. Combined with the effect of the insulation material at the bottom, it becomes possible to design the container based on its strength at high temperatures, a so-called "small wall design."

現今主流となっている大型低圧のメタノール合成装置に
も、このアンモニア合成装置と同様の設計が適用できる
。A similar design to this ammonia synthesis device can be applied to large, low-pressure methanol synthesis devices that are currently mainstream.

以上詳細に説明したように、本発明によって極めて簡単
な多孔管を使用することにより、圧力降下が非常に少い
半径流反応装置を低コストで実現することができる。As explained in detail above, by using a very simple perforated tube according to the present invention, a radial flow reactor with a very low pressure drop can be realized at low cost.

この発明は触媒を充填する反応装置に広く適用できるが
、特に中、大型の反応装置、吸着装置に好適である。The present invention can be widely applied to reaction apparatuses filled with catalysts, but is particularly suitable for medium to large-sized reaction apparatuses and adsorption apparatuses.

【図面の簡単な説明】[Brief explanation of drawings]

第１図　従来装置の説明図 （ａ）軸流反応装置 （ｂ）半径流反応装置、上下仕切り板装備（Ｃ）半径流
反応装置、上仕切り板省略第２図　本発明に使用可能な
種々の多孔管断面図（ａ）円形管 （ｂ）山形鋼および蓋 （Ｃ）溝形鋼および蓋 （ｄ　）半割円形管および蓋 （ｅ）突起つき円形管 （Ｍ、（ｃ＋　）　多孔板 第３図　本発明を適用した反応装置断面図第４図　本発
明を適用したアンモニア合成装置断面図 １　反応容器 ２　上部鏡板 ３　下部鏡板 ４　多孔管 ５　内部バスケット ６　触媒 ７　断熱材 ８　非触媒、非吸着質充填物 ９　原料ガス入口 １０　反応カス出口 １１　熱交換器 東洋エンジニアリング株式会社 ヤ１図 ヤ２１児 ＜ｆ＞　＜３） １＝二二」−１＝＝工＝＝ンFig. 1 Explanatory diagram of a conventional device (a) Axial flow reactor (b) Radial flow reactor, equipped with upper and lower partition plates (C) Radial flow reactor, upper partition plate omitted Fig. 2 Various types that can be used in the present invention Cross-sectional view of perforated tube (a) Circular tube (b) Angle steel and lid (C) Channel steel and lid (d) Half-split circular tube and lid (e) Circular tube with protrusion (M, (c+) Perforated plate No. 3 Figure 4 Cross-sectional view of a reaction device to which the present invention is applied Figure 4 Cross-sectional view of an ammonia synthesis device to which the present invention is applied 1 Reaction vessel 2 Upper head plate 3 Lower head plate 4 Porous tube 5 Internal basket 6 Catalyst 7 Heat insulating material 8 Non-catalyst, non-adsorbent Filler 9 Raw material gas inlet 10 Reaction residue outlet 11 Heat exchanger Toyo Engineering Co., Ltd.

Claims (5)

【特許請求の範囲】[Claims] （１）ガス状原料を固定層固体触媒あるいは吸着剤と接
触させ、反応あるいは吸着を生起せしめる竪型反応また
は吸着装置であって、原料ガスの全部あるいは大部分が
触媒あるいは吸着剤層外側側面から略半径方向に流れて
、反応または吸着容器の中心軸と同軸に設けられた内側
バスケットに流入する、またはこの逆の方向に流れる、
反応または吸着装置において、 反応または吸着容器の内壁に接して、触媒あるいは吸着
剤層上部空間から触媒あるいは吸着剤層下端に達し、上
端が触媒あるいは吸着剤層上部空間に開いている多くの
多孔管または多孔板または高空間率充填物が、該反応ま
たは吸着容器の内壁上に均等に鉛直に設けられているこ
とを特徴とする、半径流反応または吸着装置。(1) A vertical reaction or adsorption device in which a gaseous raw material is brought into contact with a fixed bed solid catalyst or adsorbent to cause reaction or adsorption, and all or most of the raw material gas comes from the outside side of the catalyst or adsorbent layer. flowing generally radially into an inner basket coaxial with the central axis of the reaction or adsorption vessel, or in the opposite direction;
In a reaction or adsorption device, many porous tubes are in contact with the inner wall of the reaction or adsorption vessel, reaching from the space above the catalyst or adsorbent layer to the bottom end of the catalyst or adsorbent layer, and whose upper end is open to the space above the catalyst or adsorption layer. or a radial flow reaction or adsorption device, characterized in that a perforated plate or a high porosity packing is vertically provided evenly on the inner wall of the reaction or adsorption vessel. （２）該内側バスケットはその側面、または側面および
上面が、ガスが通過可能につくられており、その上端が
触媒あるいは吸着剤層中に、該多孔管または多孔板また
は高空間率充填物から該内側バスケットまでの距離に略
等しい深さに埋っているように設置されている、特許請
求の範囲第１項に記載の半径流反応または吸着装置。(2) The inner basket has a side surface, or a side surface and an upper surface, which are formed to allow gas to pass through, and the upper end of the inner basket is formed from the perforated tube, perforated plate, or high porosity packing into the catalyst or adsorbent layer. The radial flow reaction or adsorption device according to claim 1, wherein the radial flow reaction or adsorption device is installed to be buried at a depth approximately equal to the distance to the inner basket. （３）触媒あるいは吸着剤層の上面が、−該内側バスケ
ットの上端中心を中心とし、そこまでの触媒あるいは吸
着剤層の深さを半径とする球面と略同じように充填され
、触媒あるいは吸着剤層上端中心を通る水平面と触媒あ
るいは吸着斉１層上面との間には、カス通過抵抗の小さ
い非触媒あるいは非吸着質充填物が充填されている、特
許請求の範囲第１項または第２項に記載の半径流反応ま
たは吸着装置。(3) The upper surface of the catalyst or adsorbent layer is packed so that the upper surface of the catalyst or adsorbent layer is filled in the same way as a sphere whose center is the center of the upper end of the inner basket and whose radius is the depth of the catalyst or adsorbent layer up to that point. Claim 1 or 2, wherein a non-catalyst or non-adsorbent packing having low resistance to passing through the residue is filled between a horizontal plane passing through the center of the upper end of the agent layer and the upper surface of the catalyst or adsorption layer. A radial flow reaction or adsorption device as described in Section. （４）触媒あるいは吸着剤が反応または吸着容器、該多
孔管または多孔板または高空間率充填物、および該内側
バスケットの間の空間に、反応または吸着容器下部鏡板
の上に直接、あるいは下部鏡板の上に置かれた断熱材の
上に充填されている、特許請求の範囲第１項ないし第３
項のいずれかに記載の半径流反応または吸着装置。(4) The catalyst or adsorbent is present in the space between the reaction or adsorption vessel, the perforated tube or plate or the high void ratio packing, and the inner basket, directly on the lower head plate of the reaction or adsorption vessel, or directly on the lower head plate of the reaction or adsorption vessel. Claims 1 to 3 are filled on top of the heat insulating material placed on top of the heat insulating material.
A radial flow reaction or adsorption device according to any of paragraphs. （５）冷却熱媒体が内部を流通する多数の冷却管が、触
媒あるいは吸着剤層中にその略全長にわたり垂直に、反
応または吸着容器の中心軸と中心を同じくする同心円上
に、夫々等間隔に配列されている、特許請求の範囲第１
項な□いし第４項に記載の半径流反応または吸着装置。(5) A large number of cooling pipes through which a cooling heat transfer medium flows are arranged vertically over almost the entire length of the catalyst or adsorbent layer, and arranged at equal intervals on a concentric circle whose center is the same as the central axis of the reaction or adsorption vessel. Claim 1 arranged in
The radial flow reaction or adsorption device according to items □ to 4.
JP58247925A 1983-12-26 1983-12-26 Apparatus for reaction or adsorption due to radius flow Granted JPS60137431A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP58247925A JPS60137431A (en) 1983-12-26 1983-12-26 Apparatus for reaction or adsorption due to radius flow

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP58247925A JPS60137431A (en) 1983-12-26 1983-12-26 Apparatus for reaction or adsorption due to radius flow

Publications (2)

Publication Number Publication Date
JPS60137431A true JPS60137431A (en) 1985-07-22
JPH0135690B2 JPH0135690B2 (en) 1989-07-26

Family

ID=17170582

Family Applications (1)

Application Number Title Priority Date Filing Date
JP58247925A Granted JPS60137431A (en) 1983-12-26 1983-12-26 Apparatus for reaction or adsorption due to radius flow

Country Status (1)

Country Link
JP (1) JPS60137431A (en)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6456132A (en) * 1987-05-20 1989-03-03 Haldor Topsoe As Module manifold means for distribution of gas stream in reactor
US5632807A (en) * 1993-06-03 1997-05-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device for the separation of elements of a gas mixture by adsorption
US5716427A (en) * 1995-08-21 1998-02-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Equipment for gas separation by adsorption
US5873929A (en) * 1996-07-02 1999-02-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Gas treatment bottle
US6129780A (en) * 1998-02-26 2000-10-10 L'air Liquide Process and device for purification of gas by adsorption with fixed horizontal beds
US6280508B1 (en) * 1998-01-07 2001-08-28 The Boc Group Plc PSA systems
JP2013255888A (en) * 2012-06-13 2013-12-26 Toyota Motor Corp Impurity removing apparatus
EP3219384A1 (en) * 2016-03-16 2017-09-20 Casale SA Walls for catalytic beds of radial- or axial-flow reactors
CN108295627A (en) * 2018-01-04 2018-07-20 中石化上海工程有限公司 Drying tower for gas dry
JP2022089796A (en) * 2020-12-04 2022-06-16 グク イ、サン Radial flow reactor

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6456132A (en) * 1987-05-20 1989-03-03 Haldor Topsoe As Module manifold means for distribution of gas stream in reactor
US5632807A (en) * 1993-06-03 1997-05-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device for the separation of elements of a gas mixture by adsorption
US5716427A (en) * 1995-08-21 1998-02-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Equipment for gas separation by adsorption
US5873929A (en) * 1996-07-02 1999-02-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Gas treatment bottle
US6280508B1 (en) * 1998-01-07 2001-08-28 The Boc Group Plc PSA systems
US6129780A (en) * 1998-02-26 2000-10-10 L'air Liquide Process and device for purification of gas by adsorption with fixed horizontal beds
JP2013255888A (en) * 2012-06-13 2013-12-26 Toyota Motor Corp Impurity removing apparatus
EP3219384A1 (en) * 2016-03-16 2017-09-20 Casale SA Walls for catalytic beds of radial- or axial-flow reactors
WO2017157717A1 (en) * 2016-03-16 2017-09-21 Casale Sa Walls for catalytic beds of radial- or axial-flow reactors
CN108778481A (en) * 2016-03-16 2018-11-09 卡萨尔公司 For radial flow reactors or the wall of the catalytic bed of axial flow reactor
AU2017234973B2 (en) * 2016-03-16 2021-05-27 Casale Sa Walls for catalytic beds of radial- or axial-radial flow reactors
CN108295627A (en) * 2018-01-04 2018-07-20 中石化上海工程有限公司 Drying tower for gas dry
JP2022089796A (en) * 2020-12-04 2022-06-16 グク イ、サン Radial flow reactor

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