JP3382160B2 - Reactor for gas phase polymerization of olefins - Google Patents
Reactor for gas phase polymerization of olefinsInfo
- Publication number
- JP3382160B2 JP3382160B2 JP22535998A JP22535998A JP3382160B2 JP 3382160 B2 JP3382160 B2 JP 3382160B2 JP 22535998 A JP22535998 A JP 22535998A JP 22535998 A JP22535998 A JP 22535998A JP 3382160 B2 JP3382160 B2 JP 3382160B2
- Authority
- JP
- Japan
- Prior art keywords
- reactor
- olefins
- conical lower
- inverted conical
- phase polymerization
- 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 - Fee Related
Links
Landscapes
- Polymerisation Methods In General (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Description
【発明の詳細な説明】
【０００１】
【発明の属する技術分野】本発明はオレフィン類の気相
重合用反応器に関する。
【０００２】
【従来の技術】オレフィン類の気相重合の反応器として
は、分散板を有する流動層型反応器が一般的である。し
かしながら、斯かる流動層型反応器の場合、分散板の直
上部の反応器の内壁面近傍にデッドスペース（不動部）
が形成されるためにポリマー塊が形成され易いという欠
点がある。斯かる欠点は、特開昭５８−１５４７０２号
公報にて提案された撹拌翼付流動層型反応器についても
同様に生じる。
【０００３】そこで、反応器の内壁面と分散板との隅部
に傾斜を有するダミーを挿入した構造の反応器（特開昭
５８−１４５７０２号公報）、分散板より上部の反応器
の内径が分散板より下部の反応器の内径に比して小さく
された反応器（特開昭６２−２７５１０７号公報）等が
提案されている。しかしながら、斯かる構造の反応器は
構造が複雑であり、施工が困難である。
【０００４】
【発明が解決しようとする課題】本発明は、上記実情に
鑑みなされたものであり、その目的は、比較的簡単な構
造であって、安定した連続気相重合が可能である、オレ
フィン類の気相重合用反応器を提供することにある。
【０００５】
【課題を解決するための手段】すなわち、本発明の要旨
は、逆円錐形下部（１）と円筒形上部（２）とから成る
反応器本体（３）、逆円錐形下部（１）に設けられた原
料オレフィン供給管（４）、円筒形上部（２）に必要に
応じて設けられた製品ポリマー排出管（５）、反応器本
体（３）の内部に配置され且つ上記の逆円錐形下部
（１）の断面形状に倣ったＶ字形状の撹拌翼（６）が備
えられた撹拌軸（７）から成り、逆円錐形下部の頂角
（α）とＶ字形状の撹拌翼の頂角（β）が同一であり且
つ４５〜９０°の範囲であることを特徴とする、オレフ
ィン類の気相重合用反応器に存する。
【０００６】
【発明の実施の形態】以下、本発明を添付図面に基づい
て詳細に説明する。図１は、本発明のオレフィン類の気
相重合用反応器（以下、単に「反応器」と略記する）の
一例の概念説明図である。
【０００７】本発明の反応器（１０）は、逆円錐形下部
（１）と円筒形上部（２）とから成る反応器本体
（３）、原料オレフィン供給管（４）、製品ポリマー排
出管（５）、撹拌翼（６）を備えた撹拌軸（７）から主
として構成される。
【０００８】逆円錐形下部（１）の頂角（α）は、４５
〜９０°の範囲とされる。頂角（α）が４５°未満の場
合は、高さの割に内容積が小さくなるため経済的ではな
く、また、９０°を超える場合は、ポリマーのデッドス
ペースが形成される。逆円錐形下部（１）と円筒形上部
（２）との高さ方向の比率は、１：０．５〜２の範囲が
好ましく、反応器本体（３）の内容積は、通常、１Ｌか
ら１０ｍ3の範囲とされる。
【０００９】原料オレフィン供給管（４）は、逆円錐形
下部（１）に設けられる。図示した例の場合、原料オレ
フィン供給管（４）は、好ましい態様として、逆円錐形
下部（１）の底部（頂部）に開口して設けられている。
製品ポリマー排出管（５）は、円筒形上部（２）に必要
に応じて設けられる。図示した例の場合、製品ポリマー
排出管（５）の基端側が反応器本体（３）内に挿入され
且つ基端側の開口部が逆円錐形下部（１）と円筒形上部
（２）との接合部付近に位置されている。オレフィン類
の気相重合が連続的に実施される場合、製品ポリマー排
出管（５）は未反応オレフィン回収管としても機能す
る。また、オレフィン類の気相重合が回分的に実施され
る場合、製品ポリマーは各種の手段で抜き出すことが出
来るため、製品ポリマー排出管（５）は必ずしも必要で
はない。なお、図中の符号（８）は必要に応じて円筒形
上部（２）に設けられた触媒供給管である。
【００１０】撹拌翼（６）が備えられた撹拌軸（７）
は、反応器本体（３）の内部に配置される。そして、撹
拌翼（６）は、例えば細幅板状部材または棒状部材にて
形成され、円錐形下部（１）の断面形状に倣ったＶ字形
状を有しており、その頂角（β）は、逆円錐形下部
（１）の頂角（α）と同一であり且つ４５〜９０°の範
囲とされる。その結果、逆円錐形下部（１）の場合と同
様にポリマーのデッドスペースの形成が防止される。逆
円錐形下部（１）とＶ字形状の撹拌翼（６）との間に形
成されるクリアランスは、ポリマーの付着防止の観点か
ら、可及的に小さくするのが好ましく、具体的には、３
０ｍｍ以下が好ましく、１０ｍｍ以下が更に好ましい。
また、Ｖ字形状の撹拌翼（６）の左右の各部の長さは、
その先端部が逆円錐形下部（１）の傾斜内壁面の基部と
同一高さに位置する程度が好ましい。
【００１１】図示した例の場合、撹拌軸（７）は、好ま
しい態様として、コの字形先端部を備え、当該先端部の
二股軸部（７ａ）及び（７ｂ）によってＶ字形状の撹拌
翼（６）の左右の各部を固定した構造を有している。斯
かる構造によれば、十分な周速で回転する二股軸部（７
ａ）及び（７ｂ）で撹拌翼固定軸が構成されるため、撹
拌翼固定軸へのポリマーの溶融付着が防止されて重合が
安定化される。二股軸部（７ａ）及び（７ｂ）の距離
（Ｌ1）は、円筒形上部（２）の直径（Ｌ2）に対し、通
常１／３倍以上、好ましくは１／２倍以上とされる。な
お、図示を省略したが、原料オレフィン供給管（４）、
製品ポリマー排出管（５）、触媒供給管（８）の適宜の
箇所（通常は管の途中）には、流量調節などの目的で所
定のバルブが設けられる。
【００１２】本発明の反応器で重合されるオレフィン類
としては、エチレン、プロピレン、１−ブテン、１−ヘ
キセン等が挙げられる。これらのオレフィン類の１種ま
たは２種以上は、Ｈ2ガス等と混合され、原料ガスとし
て原料オレフィン供給管（４）から供給される。触媒と
しては、ＴｉやＭｇを主成分とする所謂チグラー・ナッ
ター触媒、メタロセン系遷移金属を主成分とする触媒な
どが使用される。また、助触媒としては、トリアルキル
アルミニウム、アルモキサン等が使用される。触媒およ
び助触媒は、例えば触媒供給管（８）から固体状または
スラリー状で供給される。この際、キャリヤーガスとし
て、Ｎ2、Ａｒ等の不活性ガスを使用してもよい。ま
た、助触媒は、原料オレフィン供給管（４）から供給さ
れる原料ガスに同伴させて供給することも出来る。
【００１３】重合温度は通常６０〜１２０℃、重合圧力
は通常０．５〜５ＭＰａ、連続重合の場合の原料ガスの
供給速度は、円筒形上部（２）における空塔速度として
通常０．１〜１０ｃｍｓとされる。なお、重合反応に伴
って生じる反応熱は、原料ガスの顕熱に利用されて除熱
される。斯かる除熱は、撹拌翼（６）の撹拌効果によっ
て促進される。また、連続重合の場合の反応器本体
（３）内のポリマーのホールド量は、円筒形上部（２）
の内壁面へのポリマーの付着を防止する観点から、逆円
錐形下部（１）を満たす範囲までとするのが好ましい。
【００１４】
【発明の効果】以上説明した本発明によれば、比較的簡
単な構造であって、安定した連続気相重合が可能であ
る、オレフィン類の気相重合用反応器が提供され、本発
明の工業的価値は顕著である。Description: TECHNICAL FIELD The present invention relates to a reactor for gas phase polymerization of olefins. [0002] As a reactor for gas phase polymerization of olefins, a fluidized bed reactor having a dispersion plate is generally used. However, in the case of such a fluidized bed reactor, a dead space (immovable portion) near the inner wall surface of the reactor immediately above the dispersion plate.
However, there is a disadvantage that a polymer mass is easily formed due to the formation of Such a drawback similarly occurs in the fluidized bed reactor with a stirring blade proposed in Japanese Patent Application Laid-Open No. 58-154702. Therefore, a reactor having a structure in which an inclined dummy is inserted at the corner between the inner wall surface of the reactor and the dispersion plate (JP-A-58-145702), the inner diameter of the reactor above the dispersion plate is increased. A reactor which is smaller than the inner diameter of the reactor below the dispersion plate (Japanese Patent Application Laid-Open No. 62-275107) and the like have been proposed. However, such a reactor has a complicated structure and is difficult to construct. SUMMARY OF THE INVENTION [0004] The present invention has been made in view of the above-mentioned circumstances, and has as its object a relatively simple structure capable of performing stable continuous gas-phase polymerization. An object of the present invention is to provide a reactor for gas phase polymerization of olefins. That is, the gist of the present invention is to provide a reactor body (3) comprising an inverted conical lower part (1) and a cylindrical upper part (2), and an inverted conical lower part (1). ), A product polymer discharge pipe (5) provided as needed in the cylindrical upper part (2), and the inside of the reactor body (3). Consisting of a stirring shaft (7) provided with a V-shaped stirring blade (6) following the cross-sectional shape of the conical lower portion (1), the apex angle (α) of the inverted conical lower portion and the V-shaped stirring blade. Have the same apex angle (β) and are in the range of 45 to 90 °. Hereinafter, the present invention will be described in detail with reference to the accompanying drawings. FIG. 1 is a conceptual explanatory view of an example of a reactor for gas-phase polymerization of olefins of the present invention (hereinafter simply referred to as “reactor”). The reactor (10) of the present invention comprises a reactor body (3) comprising an inverted conical lower part (1) and a cylindrical upper part (2), a raw olefin supply pipe (4), and a product polymer discharge pipe ( 5), mainly comprising a stirring shaft (7) provided with a stirring blade (6). The apex angle (α) of the inverted conical lower part (1) is 45
９０90 °. When the apex angle (α) is less than 45 °, the internal volume is small for the height, which is not economical. When it is more than 90 °, a dead space of the polymer is formed. The ratio of the inverted conical lower part (1) to the cylindrical upper part (2) in the height direction is preferably in the range of 1: 0.5 to 2, and the internal volume of the reactor body (3) is usually from 1 L to 1 L. The range is 10 m 3 . The raw olefin supply pipe (4) is provided in the inverted conical lower part (1). In the case of the illustrated example, the raw material olefin supply pipe (4) is, as a preferred embodiment, provided so as to open at the bottom (top) of the inverted conical lower part (1).
The product polymer discharge pipe (5) is provided on the cylindrical upper part (2) as needed. In the illustrated example, the proximal end of the product polymer discharge pipe (5) is inserted into the reactor body (3) and the proximal opening has an inverted conical lower part (1) and a cylindrical upper part (2). Near the junction. When the gas phase polymerization of olefins is continuously performed, the product polymer discharge pipe (5) also functions as an unreacted olefin recovery pipe. When the gas phase polymerization of olefins is carried out batchwise, the product polymer can be extracted by various means, and thus the product polymer discharge pipe (5) is not necessarily required. Reference numeral (8) in the drawing denotes a catalyst supply pipe provided on the cylindrical upper part (2) as necessary. [0010] A stirring shaft (7) provided with a stirring blade (6).
Is located inside the reactor body (3). The stirring blade (6) is formed of, for example, a narrow plate-like member or a rod-like member, has a V-shape following the cross-sectional shape of the conical lower part (1), and has an apex angle (β). Is the same as the apex angle (α) of the inverted conical lower part (1) and is in the range of 45 to 90 °. As a result, formation of a dead space of the polymer is prevented as in the case of the inverted conical lower part (1). The clearance formed between the inverted conical lower part (1) and the V-shaped stirring blade (6) is preferably made as small as possible from the viewpoint of preventing the polymer from adhering. 3
0 mm or less is preferable, and 10 mm or less is more preferable.
Also, the length of each part on the left and right of the V-shaped stirring blade (6) is
It is preferable that the tip is located at the same height as the base of the inclined inner wall surface of the inverted conical lower part (1). In the case of the illustrated example, the stirring shaft (7) preferably has a U-shaped tip, and the V-shaped stirring blade (7) is formed by the forked shafts (7a) and (7b) of the tip. 6) has a structure in which the left and right parts are fixed. According to such a structure, the forked shaft (7) rotating at a sufficient peripheral speed is used.
Since the fixed shaft of the stirring blade is configured by a) and (7b), the polymer is prevented from being adhered to the fixed shaft of the stirring blade by melting, and the polymerization is stabilized. The distance (L1) between the forked shaft portions (7a) and (7b) is usually at least 1/3 times, preferably at least 1/2 times, the diameter (L2) of the cylindrical upper portion (2). Although not shown, the raw material olefin supply pipe (4),
A predetermined valve is provided at an appropriate place (usually in the middle of the pipe) of the product polymer discharge pipe (5) and the catalyst supply pipe (8) for the purpose of flow rate adjustment and the like. The olefins polymerized in the reactor of the present invention include ethylene, propylene, 1-butene, 1-hexene and the like. One or more of these olefins are mixed with H 2 gas or the like and supplied as a raw material gas from a raw olefin supply pipe (4). As the catalyst, a so-called Ziegler-Natta catalyst containing Ti or Mg as a main component, a catalyst containing a metallocene transition metal as a main component, or the like is used. Further, as the co-catalyst, trialkylaluminum, alumoxane or the like is used. The catalyst and the cocatalyst are supplied, for example, in a solid or slurry form from a catalyst supply pipe (8). At this time, an inert gas such as N 2 or Ar may be used as the carrier gas. Further, the co-catalyst can be supplied together with the raw material gas supplied from the raw olefin supply pipe (4). The polymerization temperature is usually 60 to 120 ° C., the polymerization pressure is usually 0.5 to 5 MPa, and the feed rate of the raw material gas in the case of continuous polymerization is usually 0.1 to 0.1 as the superficial velocity in the cylindrical upper part (2). 10 cms. The reaction heat generated by the polymerization reaction is utilized as sensible heat of the raw material gas and is removed. Such heat removal is promoted by the stirring effect of the stirring blade (6). In the case of continuous polymerization, the hold amount of the polymer in the reactor body (3) is limited to the cylindrical upper part (2).
From the viewpoint of preventing the polymer from adhering to the inner wall surface, it is preferable that the thickness be within a range satisfying the inverted conical lower portion (1). According to the present invention described above, there is provided a reactor for gas phase polymerization of olefins, which has a relatively simple structure and enables stable continuous gas phase polymerization. The industrial value of the present invention is significant.
【図面の簡単な説明】
【図１】本発明のオレフィン類の気相重合用反応器の一
例の概念説明図
【符号の説明】
１：逆円錐形下部
２：円筒形上部
３：反応器本体
４：原料オレフィン供給管
５：製品ポリマー排出管
６：撹拌翼
７：撹拌軸
８：触媒供給管BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a conceptual explanatory view of an example of a reactor for gas-phase polymerization of olefins of the present invention [Description of symbols] 1: Inverted conical lower part 2: Cylindrical upper part 3: Reactor body 4: raw material olefin supply pipe 5: product polymer discharge pipe 6: stirring blade 7: stirring shaft 8: catalyst supply pipe
Claims (1)
とから成る反応器本体（３）、逆円錐形下部（１）に設
けられた原料オレフィン供給管（４）、円筒形上部
（２）に必要に応じて設けられた製品ポリマー排出管
（５）、反応器本体（３）の内部に配置され且つ上記の
逆円錐形下部（１）の断面形状に倣ったＶ字形状の撹拌
翼（６）が備えられた撹拌軸（７）から成り、逆円錐形
下部の頂角（α）とＶ字形状の撹拌翼の頂角（β）が同
一であり且つ４５〜９０°の範囲であることを特徴とす
る、オレフィン類の気相重合用反応器。(1) Inverted conical lower part (1) and cylindrical upper part (2)
(3), a raw material olefin supply pipe (4) provided in the inverted conical lower part (1), and a product polymer discharge pipe (5) provided as necessary in the cylindrical upper part (2). A stirring shaft (7) provided inside the reactor body (3) and provided with a V-shaped stirring blade (6) following the cross-sectional shape of the inverted conical lower portion (1). A reactor for gas-phase polymerization of olefins, wherein the apex angle (α) of the lower part of the cone and the apex angle (β) of the V-shaped stirring blade are the same and in the range of 45 to 90 °. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22535998A JP3382160B2 (en) | 1998-07-24 | 1998-07-24 | Reactor for gas phase polymerization of olefins |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22535998A JP3382160B2 (en) | 1998-07-24 | 1998-07-24 | Reactor for gas phase polymerization of olefins |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000038406A JP2000038406A (en) | 2000-02-08 |
| JP3382160B2 true JP3382160B2 (en) | 2003-03-04 |
Family
ID=16828112
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22535998A Expired - Fee Related JP3382160B2 (en) | 1998-07-24 | 1998-07-24 | Reactor for gas phase polymerization of olefins |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3382160B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11938457B2 (en) | 2020-01-14 | 2024-03-26 | Lg Chem, Ltd. | Apparatus for preparing oligomer |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102589260A (en) * | 2012-03-08 | 2012-07-18 | 浙江汇隆化纤有限公司 | Color masterbatch scraper for filter screen |
-
1998
- 1998-07-24 JP JP22535998A patent/JP3382160B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11938457B2 (en) | 2020-01-14 | 2024-03-26 | Lg Chem, Ltd. | Apparatus for preparing oligomer |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2000038406A (en) | 2000-02-08 |
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