JP5055816B2 - Polyolefin powder transfer apparatus and method - Google Patents
Polyolefin powder transfer apparatus and method Download PDFInfo
- Publication number
- JP5055816B2 JP5055816B2 JP2006113076A JP2006113076A JP5055816B2 JP 5055816 B2 JP5055816 B2 JP 5055816B2 JP 2006113076 A JP2006113076 A JP 2006113076A JP 2006113076 A JP2006113076 A JP 2006113076A JP 5055816 B2 JP5055816 B2 JP 5055816B2
- Authority
- JP
- Japan
- Prior art keywords
- gas phase
- phase polymerization
- polymerization tank
- pressure side
- polyolefin powder
- 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.)
- Active
Links
Images
Description
本発明は、気相重合槽及び後工程用のホッパーを有するポリオレフィン製造プロセスにおいて、気相重合槽間又は気相重合槽と後工程のホッパー間のポリオレフィンパウダーの移送装置及び方法に関するものである。 The present invention relates to an apparatus and method for transferring polyolefin powder between a gas phase polymerization tank or between a gas phase polymerization tank and a post-process hopper in a polyolefin production process having a gas phase polymerization tank and a post-process hopper.
気相重合槽及び後工程用のホッパーを有するポリオレフィン製造プロセスにおいては、重合されたポリオレフィンを複数の気相重合槽間を、重合槽と次工程の重合槽との間に十分な圧力差をもたせ、移送配管中に配置された開閉弁を開閉操作を行うことにより、重合槽間の圧力差を利用してパウダーを間欠的に移送させる方法が知られている。しかし、プロピレンと他のオレフィン、例えばエチレン、１−ブテン等α−オレフィンとの共重合などで、融点が高くないプロピレン系重合体、低融点ランダムコポリマーや高耐衝撃ブロックコポリマー等の場合には、移送配管の内壁面に付着し易く、配管の閉塞を起こすおそれがある。また、反応性を未だ持っているパウダーが配管内に滞留し、そこで反応が進行して閉塞状態をつくることもある。一旦閉塞してしまうと、閉塞部を起点として閉塞状態が進行し、閉塞状態は更に悪化する。かかる状態では、移送配管を取り外し、閉塞物を取り除く必要が生じることもあり、その結果、減産や重合槽の運転の中止を余儀なくされることがある。 In a polyolefin production process having a gas phase polymerization tank and a hopper for the post-process, the polymerized polyolefin is allowed to have a sufficient pressure difference between a plurality of gas phase polymerization tanks and between the polymerization tank and the next-stage polymerization tank. A method is known in which powder is intermittently transferred using a pressure difference between polymerization tanks by opening and closing an on-off valve disposed in a transfer pipe. However, in the case of a propylene polymer having a low melting point, such as a copolymer of propylene and another olefin such as ethylene or α-olefin such as 1-butene, a low melting point random copolymer, a high impact block copolymer and the like, It tends to adhere to the inner wall surface of the transfer pipe and may cause the pipe to be blocked. In addition, the powder that still has reactivity may remain in the pipe, where the reaction proceeds to create a blocked state. Once occluded, the occluded state progresses starting from the occluded portion, and the occluded state further deteriorates. In such a state, it may be necessary to remove the transfer pipe and remove the obstruction, and as a result, it may be necessary to reduce production or stop the operation of the polymerization tank.
このような問題に対して、従来、ポリオレフィンパウダーの移送速度を高速とすることで、移送配管の閉塞防止を図ったり、移送待機中に別個に設けた洗浄ガス供給源から洗浄ガスとしてプロピレンを移送配管に導入して、移送配管内の滞留パウダーを押し流して移送配管の閉塞防止を図っている（特許文献１参照）。また、特別な洗浄ガス源を設けずに気相重合槽の循環ガスを取り出し昇圧して、洗浄ガスとして用いる方法（特許文献２参照）、さらに、高圧側の抜出し弁の開閉、洗浄ガスの供給弁の開閉、循環ガスの分取弁の開閉を順次繰り返して間欠的にポリオレフィンを移送する方法（特許文献３参照）等が提案されてきた。しかし、これらの方法によっても、循環ガスの昇圧設備が必要であることや洗浄ガスの圧力によっては移送配管の洗浄が十分に行われないこと等の問題があり、さらに改良が望まれていた。 In order to solve such problems, conventionally, the transfer speed of polyolefin powder is increased to prevent clogging of the transfer pipe, or propylene is transferred as a cleaning gas from a separate cleaning gas supply source during standby for transfer. It introduce | transduces into piping and the staying powder in transfer piping is washed away and the blockage | blocking of transfer piping is prevented (refer patent document 1). Also, a method of taking out and raising the pressure of the circulating gas in the gas phase polymerization tank without providing a special cleaning gas source and using it as a cleaning gas (see Patent Document 2), opening and closing of the high-pressure side extraction valve, and supply of the cleaning gas There has been proposed a method of intermittently transferring polyolefin by sequentially opening and closing a valve and opening and closing a circulating gas fractionation valve (see Patent Document 3). However, these methods also have problems such as the need for a circulating gas pressurization facility and the insufficient cleaning of the transfer pipe depending on the pressure of the cleaning gas, and further improvements have been desired.
かかる実情に鑑み、本発明の目的は、ポリオレフィンパウダーの移送に際して、移送配管の洗浄用ガスが不要で、かつ、移送配管へのポリオレフィンパウダーの付着や閉塞を生じることのない、効率のよいポリオレフィンパウダーの移送装置及び方法を提供することにある。 In view of such circumstances, an object of the present invention is to provide an efficient polyolefin powder that does not require cleaning gas for the transfer pipe and does not cause the polyolefin powder to adhere to or clog the transfer pipe when transferring the polyolefin powder. It is providing the transfer apparatus and method of this.
すなわち本発明は、
（１）高圧側の気相重合槽と、低圧側の次工程の気相重合槽又は後工程用ホッパーと、高圧側の気相重合槽から次工程の気相重合槽又は後工程用ホッパーへの移送配管とを有するポリオレフィンパウダーの移送装置であって、
高圧側の気相重合槽から、低圧側の次工程の気相重合槽又は後工程用ホッパーへの移送配管が、水平部分を有しないように常に勾配をもたせて設けられ、かつ、高圧側の気相重合槽はポリオレフィン抜出し口を有し、該気相重合槽のポリオレフィン抜出し口に自動連続抜出し弁が設けられたポリオレフィンパウダーの移送装置、
（２）前記移送配管の勾配が１０°〜９０°の勾配を有することを特徴とする（１）のポリオレフィンパウダーの移送装置、
（３）前記自動連続抜き出し弁がＶノッチディスクタイプのボール弁である（１）、（２）のポリオレフィンパウダー移送装置、
（４）前記移送配管のサイズが２インチ以上である（１）、（２）、（３）のポリオレフィンパウダーの移送装置、
（５）流動層部分を有する高圧側の気相重合槽においてポリオレフィンパウダーを製造し、当該高圧側の気相重合槽から低圧側の次工程の気相重合槽又は後工程用ホッパーへ、ポリオレフィンパウダーを移送するポリオレフィン製造プロセスにおいて、下記Ａ工程及びＢ工程を含むポリオレフィンパウダーの移送方法、
Ａ工程：高圧側の気相重合槽から、低圧側の次工程の気相重合槽又は後工程用ホッパーへ、水平部分を有しないように常に勾配をもたせて設けられた移送配管を通じてポリオレフィンパウダーを移送する工程
Ｂ工程：前記の高圧側の気相重合槽のポリオレフィンパウダー抜出し口に設けられた自動連続抜出し弁を、当該高圧側の気相重合槽の流動層レベルを一定に保つように制御し、ポリオレフィンパウダーを低圧側の次工程の気相重合槽又は後工程用ホッパーへ連続的に移送する工程。
（６）前記高圧側の気相重合槽内の圧力と、前記低圧側の気相重合槽又は後工程用のホッパーとの間の圧力差が１５０ｋＰａ〜３０００ｋＰａである（６）のポリオレフィンパウダーの移送方法。
（７）前記自動連続抜き出し弁がＶノッチディスクタイプのボール弁である（５）、（６）のポリオレフィンパウダーの移送方法。
（８）前記移送配管のサイズが２インチ以上である（５）、（６）、（７）のポリオレフィンパウダーの移送方法、
（９）前記ポリオレフィンパウダーがエチレン又はプロピレンの単独重合体もしくはエチレン、プロピレン、１−ブテンから選ばれる２以上の共重合体であることを特徴とする（５）、（６）、（７）、（８）のポリオレフィンパウダーの移送方法
（１０）前記（５）、（６）、（７）、（８）、（９）のポリオレフィンパウダーの移送方法によりポリオレフィンパウダーを移送する工程を含むポリオレフィンの製造方法、に係るものである。
That is, the present invention
(1) Gas phase polymerization tank on the high pressure side, gas phase polymerization tank or post-process hopper on the low pressure side, and gas phase polymerization tank on the high pressure side to the gas phase polymerization tank or post process hopper on the next process A polyolefin powder transfer device having a transfer pipe of
The transfer piping from the high-pressure side gas phase polymerization tank to the low-pressure side next-stage gas phase polymerization tank or the post-process hopper is always provided with a gradient so as not to have a horizontal portion, and on the high-pressure side A gas phase polymerization tank has a polyolefin extraction port, and a polyolefin powder transfer device provided with an automatic continuous extraction valve at the polyolefin extraction port of the gas phase polymerization tank,
(2) The polyolefin powder transfer device according to (1), wherein the transfer pipe has a gradient of 10 ° to 90 °,
(3) The polyolefin powder transfer device according to (1) or (2), wherein the automatic continuous extraction valve is a V-notch disk type ball valve,
(4) The polyolefin powder transfer device according to (1), (2), or (3), wherein the size of the transfer pipe is 2 inches or more,
(5) Polyolefin powder is produced in a high-pressure side gas phase polymerization tank having a fluidized bed portion, and is transferred from the high-pressure side gas phase polymerization tank to the low-pressure side next-stage gas phase polymerization tank or a post-process hopper. In the polyolefin production process of transferring the polyolefin powder, a method for transferring polyolefin powder comprising the following step A and step B,
Process A: Polyolefin powder is fed from a high-pressure side gas phase polymerization tank to a low-pressure side next-stage gas phase polymerization tank or a post-process hopper through a transfer pipe that is always provided with a gradient so as not to have a horizontal portion. Step B of transferring: The automatic continuous extraction valve provided at the polyolefin powder extraction port of the high pressure side gas phase polymerization tank is controlled so as to keep the fluidized bed level of the high pressure side gas phase polymerization tank constant. The step of continuously transferring the polyolefin powder to the gas phase polymerization tank or the post-process hopper of the next step on the low pressure side.
(6) Transfer of polyolefin powder according to (6), wherein the pressure difference between the pressure in the gas phase polymerization tank on the high pressure side and the gas phase polymerization tank on the low pressure side or a hopper for a post process is 150 kPa to 3000 kPa. Method.
(7) The method for transferring polyolefin powder according to (5) and (6), wherein the automatic continuous extraction valve is a V-notch disk type ball valve.
(8) The method for transferring polyolefin powder according to (5), (6), (7), wherein the size of the transfer pipe is 2 inches or more,
(9) The polyolefin powder is a homopolymer of ethylene or propylene or a copolymer of two or more selected from ethylene, propylene and 1-butene (5), (6), (7), (8) Polyolefin powder transfer method (10) Production of polyolefin including the step of transferring polyolefin powder by the polyolefin powder transfer method of (5), (6), (7), (8), (9) Method.
本発明により、ポリオレフィンパウダーの移送に際して、移送配管の洗浄用ガスが不要で、かつ、移送配管へのポリオレフィンパウダーの付着や閉塞を生じることのない、効率のよいポリオレフィンパウダーの移送装置及び方法の提供が可能になった。 According to the present invention, there is provided an efficient polyolefin powder transfer device and method that does not require cleaning gas for transfer piping and does not cause adhesion or blockage of polyolefin powder to the transfer piping when transferring polyolefin powder. Became possible.
以下、図面を参照しながら、本発明の好適な形態について詳細に説明する。図１は、気相重合槽から次工程のホッパーへのポリオレフィンパウダーを移送する場合の構成を概略的に示しているが、気相重合槽を複数有する場合の重合槽間の移送、重合槽とホッパー間の移送についても同様にして実施することができる。 Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. FIG. 1 schematically shows a configuration for transferring polyolefin powder from a gas phase polymerization tank to a hopper in the next step. The transfer between hoppers can be carried out in the same manner.
気相重合槽１はいわゆる流動層式であり、その内部では、オレフィンモノマーを含むガスとポリオレフィンパウダーとの混合相が形成され、この重合槽の下部に取り付けられたガス分散板の下方からの循環ガスによって流動化される。ガスの循環は、気相重合槽のトップからボトムにループ状に接続された循環ガス配管４の途中に設けられた循環ガスコンプレッサーにより循環される。循環ガス配管には、循環ガスに同伴する細かい粉体を分離するためのサイクロンと、循環ガスを冷却するための循環ガスクーラーが配置されている。気相重合槽内の混合相が流動化された状況下で、プロピレンモノマー等のオレフィン原料ガス及び触媒を気相重合槽内に供給すると、触媒の存在により重合反応が進行しポリオレフィンパウダーが製造される。このようにして製造された気相重合槽中のポリオレフィンパウダーは、気相重合槽の流動層部分から移送配管７を通して第２の気相重合槽又は次工程のホッパーに気相重合槽内の圧力によって移送される。 The gas phase polymerization tank 1 is a so-called fluidized bed type, in which a mixed phase of a gas containing an olefin monomer and a polyolefin powder is formed and circulated from below the gas dispersion plate attached to the lower part of the polymerization tank. Fluidized by gas. The gas is circulated by a circulation gas compressor provided in the middle of a circulation gas pipe 4 connected in a loop from the top to the bottom of the gas phase polymerization tank. A circulating gas pipe is provided with a cyclone for separating fine powder accompanying the circulating gas and a circulating gas cooler for cooling the circulating gas. In the situation where the mixed phase in the gas phase polymerization tank is fluidized, if an olefin source gas such as propylene monomer and a catalyst are supplied into the gas phase polymerization tank, the polymerization reaction proceeds due to the presence of the catalyst, and polyolefin powder is produced. The The polyolefin powder in the gas phase polymerization tank thus produced is transferred from the fluidized bed portion of the gas phase polymerization tank to the second gas phase polymerization tank or the hopper of the next step through the transfer pipe 7 and the pressure in the gas phase polymerization tank. Transported by
本発明の最大の特徴は、設置する移送配管７の構成である。移送配管７は、気相重合槽１から次工程の気相重合槽（図示せず）又はホッパー８へ水平部分を有しないように常に勾配をもたせて設けられる。勾配を設けることにより、移送配管の洗浄用ガスを用いることなく、ポリオレフィンパウダーの移送配管への残留、付着又は閉塞を防止することが可能になる。移送配管の勾配は、１０°〜９０°、好ましくは３０°〜９０°であり、配管サイズは２インチ以上、好ましくは３インチ以上である。
The greatest feature of the present invention is the configuration of the transfer pipe 7 to be installed. The transfer pipe 7 is always provided with a gradient so as not to have a horizontal portion from the gas phase polymerization tank 1 to the gas phase polymerization tank (not shown) or the
気相重合槽１のポリオレフィン抜出し口には、自動連続抜出し弁６を設ける。ポリオレフィンパウダーは、気相重合槽１に設けられた流動層レベル計５の信号により気相重合槽１の流動層のレベルを一定に保つように自動連続抜出し弁６を制御して移送される。
An automatic continuous extraction valve 6 is provided at the polyolefin extraction port of the gas phase polymerization tank 1. The polyolefin powder is transferred by controlling the automatic continuous extraction valve 6 so that the level of the fluidized bed in the gas phase polymerization tank 1 is kept constant by a signal from the fluidized bed level meter 5 provided in the gas phase polymerization tank 1.
レベル計としては、例えば、流動層の上下の差圧を測定する方式が採用される。自動連続抜き出し弁は、Ｖノッチディスクタイプのボール弁としてワンダー弁等が用いられる。
As the level meter, for example, a method of measuring the differential pressure above and below the fluidized bed is employed . Automatic Continuous withdrawal valves is Wonder valve or the like is Ru is used as a ball valve V-notch disk type.
移送配管の勾配をもたせ、かつ、自動連続抜き出し弁及び間欠抜き出し弁を併設することにより、ポリオレフィン製造プロセスを運転する場合のフレキシビリティーを高めることができる。例えば、必要生産量が高く高能力で設備の運転を行っている場合には、間欠抜き出し弁の開閉頻度のみでは所定の量のポリオレフィンパウダーを抜き出すのが困難であること、時間当たりの弁の開閉回数が非常に多くなり弁の短命化を招くおそれがあること等の問題があり、自動連続抜き出し弁を用いるのが好適である。また、自動連続抜き出し弁を用いて連続的に抜出しを行うことによって間欠的に抜出す場合に比べて、ポリオレフィンパウダーの移送量を低下させずに流速を、約２分の１の低速に下げ、エチレン−プロピレンブロック共重合体やプロピレン−ブテン共重合体等の粘着性ポリマーを移送する際の配管内への付着による汚れを低減することができる。一方、配管に勾配をもたせることによって、移送配管中に残留ポリマー等が滞留することがないので洗浄・排出するオレフィンモノマーガス等の洗浄ガスは不要となる。
By providing a gradient of the transfer pipe and providing an automatic continuous extraction valve and an intermittent extraction valve, flexibility in operating the polyolefin production process can be enhanced. For example, when the required production volume is high and the equipment is operating at high capacity, it is difficult to extract a predetermined amount of polyolefin powder only with the frequency of opening and closing the intermittent extraction valve, and opening and closing of the valve per hour There is a problem that the number of times becomes very large and the life of the valve may be shortened, and it is preferable to use an automatic continuous extraction valve. Moreover, compared with the case where it pulls out intermittently by performing continuous extraction using an automatic continuous extraction valve, the flow rate is lowered to a low speed of about one-half without reducing the amount of polyolefin powder transferred, It is possible to reduce contamination due to adhesion to the piping when an adhesive polymer such as an ethylene-propylene block copolymer or a propylene-butene copolymer is transferred. On the other hand, by to have a gradient in the pipe, the cleaning gas such as an olefin monomer gas for cleaning and discharging the residual polymer or the like is never you stay in transfer pipe is unnecessary.
ポリオレフィンパウダーの移送は、高圧側の気相重合槽と低圧側の第２の気相重合槽又はホッパーとの間の圧力差により行われる。この圧力差は、例えば重合槽間で移送する場合は、圧力差は４００ｋＰａ程度であるが、重合槽からホッパーへ移送する場合は、ホッパーの圧力が低いので１３００ｋＰａ程度の圧力差で移送が行われる。好ましい圧力差は、１５０ｋＰａ〜３０００ｋＰａ、より好ましくは、３００〜１５００ｋＰａである。このように、上流側の槽の圧力が１５０ｋＰａ以上高く保たれているのが好適である。圧力差が１５０ｋＰａよりも小さいと、パウダーの移送速度が不十分となる。また、圧力差が３０００ｋＰａより大きいと配管に振動が生じ、配管強度等への安全上の問題がある。 The polyolefin powder is transferred by a pressure difference between the high pressure side gas phase polymerization tank and the low pressure side second gas phase polymerization tank or hopper. For example, when the pressure difference is transferred between the polymerization tanks, the pressure difference is about 400 kPa. However, when the pressure difference is transferred from the polymerization tank to the hopper, the transfer is performed with a pressure difference of about 1300 kPa because the pressure of the hopper is low. . A preferable pressure difference is 150 kPa to 3000 kPa, more preferably 300 to 1500 kPa. Thus, it is preferable that the pressure in the upstream tank is maintained at 150 kPa or higher. When the pressure difference is smaller than 150 kPa, the powder transfer rate becomes insufficient. On the other hand, if the pressure difference is greater than 3000 kPa, vibration occurs in the piping, which causes a safety problem with respect to piping strength and the like.
本発明において、ポリオレフィンパウダーがエチレン又はプロピレンの単独重合体もしくはエチレン、プロピレン、１−ブテンから選ばれる２以上の共重合体である場合に好適に移送することができる。エチレン、プロピレン、１−ブテンから選ばれる２以上の共重合体としては、エチレン−プロピレンブロック共重合体やプロピレン−ブテン共重合体等の粘着性を有するパウダーが例示される。本発明は、これらのパウダーの移送に際して生じる、配管内の粘着性ポリマーによる汚れやパウダーの滞留を防止するのに有効であるが、エチレン又はプロピレンの単独重合体のパウダーの移送に対しても移送配管の洗浄用モノマーガスが不要であり、モノマー原単位を向上できる点で有用である。 In the present invention, when the polyolefin powder is a homopolymer of ethylene or propylene or a copolymer of two or more selected from ethylene, propylene and 1-butene, the polyolefin powder can be suitably transferred. Examples of the two or more copolymers selected from ethylene, propylene, and 1-butene include adhesive powders such as an ethylene-propylene block copolymer and a propylene-butene copolymer. The present invention is effective in preventing dirt and powder stagnation due to the adhesive polymer in the piping, which occurs during the transfer of these powders. However, the present invention is also used for the transfer of ethylene or propylene homopolymer powders. This is useful in that the monomer gas for pipe cleaning is unnecessary and the monomer basic unit can be improved.
以下、本発明を実施例に基づいて、より具体的に説明するが、もとより本発明はこれら実施例に限定されるものではない。
実施例１
図１に示した装置を用いて、エチレン‐プロピレンブロック共重合体を重合し、気相重合槽からホッパーへエチレン‐プロピレンブロック共重合体パウダーの連続移送を行った。気相重合槽とホッパーの間を長さ３０ｍ、直径５２．７ｍｍの移送配管で、配管途中には水平部分を設けず、少なくとも勾配が１０°以上となる様に接続した。気相重合槽は、圧力１．３ＭＰａ、温度７０℃、ホッパーの圧力は２０ｋＰａであり、生成エチレン‐プロピレンブロック共重合体パウダーの抜出しを、気相重合槽の流動層レベルが一定になるように自動抜出弁の開度を制御しながら行った。またその時のパウダーの流速は１１ｍ／ｓｅｃであった。配管を洗浄するモノマーガスは使用せずに２週間運転を行い、配管内部を開放点検したところ、配管内にはポリマー付着の汚れは全く見られなかった。
EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example, this invention is not limited to these Examples from the first.
Example 1
The ethylene-propylene block copolymer was polymerized using the apparatus shown in FIG. 1, and the ethylene-propylene block copolymer powder was continuously transferred from the gas phase polymerization tank to the hopper. A transfer pipe having a length of 30 m and a diameter of 52.7 mm was provided between the gas phase polymerization tank and the hopper, and a horizontal portion was not provided in the middle of the pipe, so that at least a gradient of 10 ° or more was connected. The gas phase polymerization tank has a pressure of 1.3 MPa, a temperature of 70 ° C., and a hopper pressure of 20 kPa. The extracted ethylene-propylene block copolymer powder is extracted so that the fluidized bed level of the gas phase polymerization tank is constant. This was performed while controlling the opening degree of the automatic extraction valve. The powder flow rate at that time was 11 m / sec. The monomer gas for washing the piping was used for 2 weeks without using it, and when the inside of the piping was opened and inspected, no contamination of the polymer was found in the piping.
比較例１
気相重合槽とホッパーの間を長さ７０ｍ、直径５２．７ｍｍの移送配管で、配置の関係で途中に約１０ｍの水平部分がある以外は、少なくとも勾配が１０°以上となる様に接続した。気相重合槽は、実施例１と同様、圧力１．３ＭＰａ、温度７０℃、ホッパーの圧力は２０ｋＰａであったが、配管洗浄ガスとしてプロピレンモノマーを８００ｋｇ／Ｈで流し、間欠的に抜出しを行いながら気相重合槽からホッパーへエチレン‐プロピレンブロック共重合体パウダーの移送を行った。
パウダーの間欠抜出しは、弁を３０〜４０ｓｅｃ開、１０ｓｅｃ閉の周期で行い、弁が閉じられている間は洗浄モノマーガスを供給した。抜出し時のパウダー流速は２１ｍ／ｓｅｃであった。１週間の運転で抜出し能力が低下したので、配管内部を開放点検したところ、配管内にはポリマーが付着し、汚れが大であった。
Comparative Example 1
Between the gas phase polymerization tank and the hopper, a transfer pipe having a length of 70 m and a diameter of 52.7 mm was connected so that the gradient was at least 10 °, except that there was a horizontal portion of about 10 m in the middle due to the arrangement. . As in Example 1, the gas phase polymerization tank had a pressure of 1.3 MPa, a temperature of 70 ° C., and a hopper pressure of 20 kPa. Propylene monomer was allowed to flow at 800 kg / H as a pipe cleaning gas, and was intermittently withdrawn. The ethylene-propylene block copolymer powder was transferred from the gas phase polymerization tank to the hopper.
The intermittent extraction of the powder was performed with a period of 30 to 40 seconds open and 10 seconds closed, and cleaning monomer gas was supplied while the valve was closed. The powder flow rate at the time of extraction was 21 m / sec. Since the extraction capacity decreased after one week of operation, the inside of the piping was inspected for openness.
上記の結果から次のことがわかる。本発明の条件に合致する実施例１は、プロピレンモノマーによる移送配管の洗浄を行わなかったにも拘わらず、２週間の運転後も移送配管内のポリオレフィンパウダーの汚れや滞留はなかった。一方、水平部分を有するポリマー移送配管を用い、間欠抜出しを行った比較例２は、配管洗浄を行ったにも拘わらず１週間でパウダーの抜出し能力が低下し、配管内のポリマーによる汚れが大きかった。 The following can be seen from the above results. In Example 1 which met the conditions of the present invention, the polyolefin powder in the transfer pipe was not soiled or retained even after the operation for 2 weeks, even though the transfer pipe was not washed with the propylene monomer. On the other hand, in Comparative Example 2 in which the polymer transfer pipe having a horizontal portion was used and intermittent extraction was performed, the powder extraction ability decreased in one week despite the pipe cleaning, and the dirt in the pipe due to the polymer was large. It was.
１…気相重合槽、２…触媒供給口、３…原料供給口、４…循環ガスライン、５…流動層レベル計、６…自動連続抜出し弁、７…移送配管、８…ホッパー、９…ガス回収ライン DESCRIPTION OF SYMBOLS 1 ... Gas phase polymerization tank, 2 ... Catalyst supply port, 3 ... Raw material supply port, 4 ... Circulating gas line, 5 ... Fluidized bed level meter, 6 ... Automatic continuous extraction valve, 7 ... Transfer piping, 8 ... Hopper, 9 ... Gas recovery line
Claims (10)
高圧側の気相重合槽から、低圧側の次工程の気相重合槽又は後工程用ホッパーへの移送配管が、水平部分を有しないように常に勾配をもたせて設けられ、かつ、高圧側の気相重合槽はポリオレフィン抜出し口を有し、該気相重合槽のポリオレフィン抜出し口に自動連続抜出し弁が設けられたポリオレフィンパウダーの移送装置。 High-pressure side gas phase polymerization tank, low-pressure side gas phase polymerization tank or post-process hopper, and transfer piping from the high-pressure side gas phase polymerization tank to the next-stage gas phase polymerization tank or post-process hopper A polyolefin powder transfer device comprising:
The transfer piping from the high-pressure side gas phase polymerization tank to the low-pressure side next-stage gas phase polymerization tank or the post-process hopper is always provided with a gradient so as not to have a horizontal portion, and on the high-pressure side A device for transferring polyolefin powder, wherein the gas phase polymerization tank has a polyolefin extraction port, and an automatic continuous extraction valve is provided at the polyolefin extraction port of the gas phase polymerization tank.
Ａ工程：高圧側の気相重合槽から、低圧側の次工程の気相重合槽又は後工程用ホッパーへ、水平部分を有しないように常に勾配をもたせて設けられた移送配管を通じてポリオレフィンパウダーを移送する工程
Ｂ工程：前記の高圧側の気相重合槽のポリオレフィンパウダー抜出し口に設けられた自動連続抜出し弁を、当該高圧側の気相重合槽の流動層レベルを一定に保つように制御し、ポリオレフィンパウダーを低圧側の次工程の気相重合槽又は後工程用ホッパーへ連続的に移送する工程。 Polyolefin powder is produced in a high-pressure side gas phase polymerization tank having a fluidized bed portion, and the polyolefin powder is transferred from the high-pressure side gas phase polymerization tank to the low-pressure side next-stage gas phase polymerization tank or a post-process hopper. In the polyolefin production process, a method for transferring polyolefin powder comprising the following step A and step B.
Process A: Polyolefin powder is fed from a high-pressure side gas phase polymerization tank to a low-pressure side next-stage gas phase polymerization tank or a post-process hopper through a transfer pipe that is always provided with a gradient so as not to have a horizontal portion. Step B of transferring: The automatic continuous extraction valve provided at the polyolefin powder extraction port of the high pressure side gas phase polymerization tank is controlled so as to keep the fluidized bed level of the high pressure side gas phase polymerization tank constant. The step of continuously transferring the polyolefin powder to the gas phase polymerization tank or the post-process hopper of the next step on the low pressure side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2006113076A JP5055816B2 (en) | 2006-04-17 | 2006-04-17 | Polyolefin powder transfer apparatus and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2006113076A JP5055816B2 (en) | 2006-04-17 | 2006-04-17 | Polyolefin powder transfer apparatus and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2007284548A JP2007284548A (en) | 2007-11-01 |
| JP5055816B2 true JP5055816B2 (en) | 2012-10-24 |
Family
ID=38756636
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2006113076A Active JP5055816B2 (en) | 2006-04-17 | 2006-04-17 | Polyolefin powder transfer apparatus and method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP5055816B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103732634B (en) * | 2011-06-21 | 2016-03-09 | 巴塞尔聚烯烃股份有限公司 | The method and apparatus of polymkeric substance is discharged by Gas-phase reactor |
| CN106432551B (en) * | 2015-08-11 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of polyacrylic method and apparatus of intermittent liquid phase bulk polymerization production |
| JP6902965B2 (en) | 2017-08-29 | 2021-07-14 | 住友化学株式会社 | Polyolefin manufacturing method |
| JP2024007084A (en) | 2022-07-05 | 2024-01-18 | 住友化学株式会社 | Polyolefin production apparatus and polyolefin production method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0574821B1 (en) * | 1992-06-18 | 1998-03-11 | Montell Technology Company bv | Process and apparatus for the gas-phase polymerization of olefins |
| FR2730999B1 (en) * | 1995-02-24 | 1997-04-18 | Bp Chemicals Snc | APPARATUS AND PROCESS FOR POLYMERIZATION OF OLEFINE IN THE GAS PHASE |
| JP2003313205A (en) * | 2002-04-19 | 2003-11-06 | Sumitomo Chem Co Ltd | Polymerizing method for polyolefin |
-
2006
- 2006-04-17 JP JP2006113076A patent/JP5055816B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| JP2007284548A (en) | 2007-11-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5055816B2 (en) | Polyolefin powder transfer apparatus and method | |
| RU2475501C2 (en) | Multi-step method for polymerisation of olefins | |
| KR100388507B1 (en) | Apparatus and process for polymering olefin in gas phase | |
| US5558472A (en) | Method and apparatus for transporting particles | |
| AU2009344862B2 (en) | Continuous fine ash depressurization system | |
| JPS5956489A (en) | Method of periodically carrying out residue produced upon gasification of ash content-containing fuel | |
| US20040258579A1 (en) | Device and method for optimising the circulation of a suspension in a plant comprising a three-phase reactor | |
| US4928739A (en) | Mold filling method and transport apparatus for bead-like resilient material transported by a fluid | |
| US6056927A (en) | Equipment and process for gas-phase olefin polymerization | |
| US20080299015A1 (en) | Apparatus and method for top removal of granular material from a fluidized bed deposition reactor | |
| HU216912B (en) | Process for continuous polimerising olefins in gas phase | |
| JP2005068207A (en) | Method of transferring polyolefin granule | |
| JP3710247B2 (en) | Gas phase polymerization equipment | |
| JP2003285928A (en) | Powdery and granular material transfer method and its device | |
| RU2289633C2 (en) | Method for processing material in the form of particles and apparatus for performing the same | |
| JPH07163856A (en) | Powder transferring method and apparatus | |
| JP7322579B2 (en) | Equipment for conveying slurry and method for conveying slurry | |
| JP4760173B2 (en) | Olefin continuous polymerization apparatus, polymer particle transfer method, and olefin polymerization method | |
| JP2006206629A (en) | Process for producing polyolefin | |
| JP5459697B2 (en) | Granule transfer pipe, olefin polymer manufacturing apparatus, powder particle transfer method, and olefin polymer manufacturing method | |
| JP2006117712A (en) | Method for producing polyolefin | |
| JP2008074949A (en) | Polymerization system of propylene-based resin | |
| JP2010195952A (en) | Manufacturing method of olefin polymer | |
| JP2010202701A (en) | Transfer method for powder, method for manufacturing olefin polymer, transfer piping, and manufacturing apparatus | |
| JPS59156487A (en) | Apparatus for phosphate-contg. water disposal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| RD05 | Notification of revocation of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7425 Effective date: 20080201 |
|
| RD05 | Notification of revocation of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7425 Effective date: 20080515 |
|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20080917 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20110527 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20110531 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20110729 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20120327 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20120522 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20120703 |
|
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20120716 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20150810 Year of fee payment: 3 |
|
| R151 | Written notification of patent or utility model registration |
Ref document number: 5055816 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R151 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20150810 Year of fee payment: 3 |
|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |