JP2007284548A - Apparatus and method for transporting polyolefin powder - Google Patents
Apparatus and method for transporting polyolefin powder Download PDFInfo
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- JP2007284548A JP2007284548A JP2006113076A JP2006113076A JP2007284548A JP 2007284548 A JP2007284548 A JP 2007284548A JP 2006113076 A JP2006113076 A JP 2006113076A JP 2006113076 A JP2006113076 A JP 2006113076A JP 2007284548 A JP2007284548 A JP 2007284548A
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- 239000000843 powder Substances 0.000 title claims abstract description 77
- 229920000098 polyolefin Polymers 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000000605 extraction Methods 0.000 claims abstract description 56
- 238000004519 manufacturing process Methods 0.000 claims abstract description 11
- 238000012685 gas phase polymerization Methods 0.000 claims description 56
- 238000006116 polymerization reaction Methods 0.000 claims description 13
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 10
- 229920000642 polymer Polymers 0.000 claims description 8
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 7
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 7
- 229920001577 copolymer Polymers 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 5
- 239000005977 Ethylene Substances 0.000 claims description 5
- -1 ethylene, propylene Chemical group 0.000 claims description 5
- 229920001519 homopolymer Polymers 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 abstract description 16
- 239000012808 vapor phase Substances 0.000 abstract description 5
- 238000012805 post-processing Methods 0.000 abstract 1
- 239000000178 monomer Substances 0.000 description 9
- 229920005676 ethylene-propylene block copolymer Polymers 0.000 description 6
- 150000001336 alkenes Chemical class 0.000 description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000011109 contamination Methods 0.000 description 3
- 239000002998 adhesive polymer Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 229920001400 block copolymer Polymers 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920005606 polypropylene copolymer Polymers 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 229920001384 propylene homopolymer Polymers 0.000 description 1
- 229920005604 random copolymer Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000004711 α-olefin Substances 0.000 description 1
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Abstract
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 prevention of transfer piping is aimed at (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 adhesion or blockage of the polyolefin powder to 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）少なくとも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、少なくとも気相重合槽から次工程の気相重合槽又はホッパーへの移送配管を、水平部分を有しないように常に勾配をもたせて設け、かつ、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及び／又は間欠抜出し弁を設けたことを特徴とするポリオレフィンパウダーの移送装置、
（２）前記次工程の気相重合槽又はホッパーへの抜出し配管の勾配が１０°〜９０°、好ましくは３０°〜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）前記連続抜き出し弁としてＶノッチディスクタイプのボール弁を設けたことを特徴とする（１）、（２）のポリオレフィンパウダー移送装置、
（４）前記間欠抜き出し弁としてオン−オフ弁を設けたことを特徴とする（１）、（２）、（３）のポリオレフィンパウダー移送装置、
（５）前記重合パウダー移送配管のサイズを２インチ以上、好ましくは３インチ以上とすることを特徴とする（１）、（２）、（３）、（４）のポリオレフィンパウダーの移送装置、
（６）少なくとも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、下記Ａ工程及びＢ工程を含む工程を有することを特徴とするポリオレフィンパウダーの移送方法、
Ａ工程：気相重合槽から次工程の気相重合槽又はホッパーへの移送配管を、水平部分を有しないように常に勾配をもたせて設け、該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及び／又は間欠抜出し弁を設け、該気相重合槽の流動層レベルを一定に保つように自動連続抜出し弁及び／又は間欠抜出し弁を制御しつつ、ポリオレフィンパウダーを連続的に低圧側の気相重合槽又は後工程用のホッパーへ移送する工程
（７）前記高圧側の気相重合槽内の圧力は、前記低圧側の気相重合槽又はは後処理工程用のホッパーの圧力より１５０ＫＰａ〜３０００ＫＰａ高く保たれていることを特徴とする（６）のポリオレフィンパウダーの移送方法。
（８）前記連続抜き出し弁としてＶノッチディスクタイプのボール弁を使用することを特徴とする（６）、（７）のポリオレフィンパウダーの移送方法。
（９） 前記間欠抜き出し弁としてオン−オフ弁を使用することを特徴とする（６）、（７）、（８）のポリオレフィンパウダーの移送方法、
（１０）前記重合パウダー移送配管のサイズを２インチ以上、好ましくは３インチ以上とすることを特徴とする（６）（７）、（８）、（９）のポリオレフィンパウダーの移送方法、
（１１）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（６）、（７）、（８）、（９）、（１０）のポリオレフィンパウダーの移送方法、に係るものである。
That is, the present invention
(1) In a polyolefin production process having at least a gas phase polymerization tank and a hopper for a post-process, always transfer pipe from at least the gas phase polymerization tank to the gas phase polymerization tank or hopper of the next step so as not to have a horizontal portion. A polyolefin powder transfer device provided with a gradient and provided with an automatic continuous extraction valve and / or an intermittent extraction valve at a polyolefin extraction port of the gas phase polymerization tank,
(2) Transfer of polyolefin powder according to (1), wherein the gradient of the extraction pipe to the gas phase polymerization tank or hopper in the next step has a gradient of 10 ° to 90 °, preferably 30 ° to 90 °. apparatus,
(3) A polyolefin powder transfer device according to (1) or (2), wherein a V-notch disc type ball valve is provided as the continuous extraction valve,
(4) A polyolefin powder transfer device according to (1), (2), or (3), wherein an on-off valve is provided as the intermittent extraction valve,
(5) The polyolefin powder transfer device of (1), (2), (3), (4), wherein the size of the polymer powder transfer pipe is 2 inches or more, preferably 3 inches or more,
(6) A polyolefin powder transfer method characterized by having a step including the following step A and step B in a polyolefin production process having at least a gas phase polymerization tank and a hopper for a post-process,
Step A: Step of transferring the polyolefin powder through the pipe from the gas phase polymerization tank to the gas phase polymerization tank or the hopper of the next step with a gradient so as not to have a horizontal portion. An automatic continuous extraction valve and / or an intermittent extraction valve are provided at the polyolefin extraction port of the gas phase polymerization tank, and the automatic continuous extraction valve and / or the intermittent extraction valve are controlled so as to keep the fluidized bed level of the gas phase polymerization tank constant. (7) The pressure in the gas phase polymerization tank on the high pressure side is the gas phase polymerization tank on the low pressure side or the step of transferring the polyolefin powder continuously to the gas phase polymerization tank on the low pressure side or the hopper for the subsequent process. Is maintained at 150 KPa to 3000 KPa higher than the pressure of the hopper for the post-treatment step. (6) The polyolefin powder transfer method according to (6).
(8) The polyolefin powder transfer method according to (6) or (7), wherein a V-notch disc type ball valve is used as the continuous extraction valve.
(9) A method for transferring polyolefin powder according to (6), (7) and (8), wherein an on-off valve is used as the intermittent extraction valve,
(10) The method for transferring polyolefin powder according to (6), (7), (8), (9), wherein the size of the polymer powder transfer pipe is 2 inches or more, preferably 3 inches or more,
(11) The polyolefin powder is a homopolymer of ethylene or propylene or a copolymer of two or more selected from ethylene, propylene and 1-butene (6), (7), (8), (9), (10) The polyolefin powder transfer method according to the present invention.
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 hopper 8 of the next step. By providing the gradient, it is possible to prevent the polyolefin powder from remaining on, attached to, or blocked from the transfer pipe without using a cleaning gas for the transfer pipe. The gradient of the transfer pipe is 10 ° to 90 °, preferably 30 ° to 90 °, and the pipe size is 2 inches or more, preferably 3 inches or more.
気相重合槽１のポリオレフィン抜出し口には、自動連続抜出し弁及び／又は間欠抜出し弁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及び／又は間欠抜出し弁６を制御して移送される。 An automatic continuous extraction valve and / or an intermittent extraction valve 6 is provided at the polyolefin extraction port of the gas phase polymerization tank 1. The polyolefin powder controls the automatic continuous extraction valve and / or the intermittent extraction valve 6 so as to keep the level of the fluidized bed in the gas phase polymerization tank 1 constant by the signal of the fluidized bed level meter 5 provided in the gas phase polymerization tank 1. Then transferred.
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。ポリオレフィン抜出し口に設ける弁は、自動連続抜き出し弁又は間欠抜き出し弁をそれぞれ単独で設けてもよいし、併設してもよい。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が連続的に流量を制御できる弁であればいずれも用いることができる。間欠抜き出し弁としては弁をオン−オフで開閉できる弁であればいずれも使用できる。オン、オフ弁とは例えば、一般のボール弁タイプのもので全開−全閉で作動させる弁のことを
指している。
As the level meter, for example, a method of measuring the differential pressure above and below the fluidized bed is adopted. As the valve provided at the polyolefin extraction port, an automatic continuous extraction valve or an intermittent extraction valve may be provided alone or in combination. As the automatic continuous extraction valve, a Wonder valve or the like is used as a V-notch disk type ball valve, but any valve can be used as long as it can continuously control the flow rate. Any intermittent extraction valve can be used as long as the valve can be opened and closed on and off. The on / off valve is, for example, a general ball valve type valve that is operated by full opening and full closing.
移送配管の勾配をもたせ、かつ、自動連続抜き出し弁又は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 or 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 providing the piping with a gradient, residual polymer or the like does not stay in the transfer piping, so that cleaning gas such as olefin monomer gas to be cleaned and discharged becomes unnecessary.
必要生産量が低く低能力で設備の運転を行っている場合には、自動抜出し弁の開度調整によるパウダー抜出しに比して、間欠的な弁の開閉による重合槽のレベル制御が容易であることや、重合槽内に塊が存在するような場合等には、連続的な抜出しにより弁開度が絞られている状態の場合に比べて、弁部分でのパウダー通過面積が大きくなること、さらに瞬間的に約２倍の高速のポリオレフィンパウダーが抜出されるので、重合槽内の塊の取り出し等が容易にできる等の理由で間欠抜き出し弁を好適に使用することができる。 When the equipment is operating with low production capacity and low capacity, it is easier to control the level of the polymerization tank by opening and closing the valve intermittently compared to powder extraction by adjusting the opening of the automatic extraction valve. In addition, when there is a lump in the polymerization tank, the powder passage area in the valve part is larger than in the state where the valve opening is reduced by continuous extraction, Furthermore, since the polyolefin powder of about twice as high speed is instantaneously extracted, the intermittent extraction valve can be suitably used for the reason that the lump in the polymerization tank can be easily taken out.
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 gas phase polymerization tank on the high pressure side and the second gas phase polymerization tank or hopper on the low pressure side. 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, the pipe is vibrated, and there is a safety problem with respect to the pipe 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. Moreover, the flow rate of the powder 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 flowed 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 during extraction was 21 m / sec. Since the extraction capacity decreased after one week of operation, the inside of the piping was inspected for openness. As a result, polymer adhered to the piping and the contamination was large.
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…自動連続抜出し弁及び／又は間欠抜出し弁、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 and / or intermittent extraction valve, 7 ... Transfer piping, 8 ... Hopper, 9 ... Gas recovery line
Claims (11)
Ａ工程：気相重合槽から次工程の気相重合槽又はホッパーへの移送配管を、水平部分を有しないように常に勾配をもたせて設け、該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及び／又は間欠抜出し弁を設け、該気相重合槽の流動層レベルを一定に保つように自動連続抜出し弁及び／又は間欠抜出し弁を制御しつつ、ポリオレフィンパウダーを連続的に低圧側の気相重合槽又は後工程用のホッパーへ移送する工程 A polyolefin powder transfer method comprising a step including the following step A and step B in a polyolefin production process having at least a gas phase polymerization tank and a hopper for a post-process.
Step A: Step of transferring the polyolefin powder through the pipe from the gas phase polymerization tank to the gas phase polymerization tank or the hopper of the next step with a gradient so as not to have a horizontal portion. An automatic continuous extraction valve and / or an intermittent extraction valve are provided at the polyolefin extraction port of the gas phase polymerization tank, and the automatic continuous extraction valve and / or the intermittent extraction valve are controlled so as to keep the fluidized bed level of the gas phase polymerization tank constant. While the polyolefin powder is continuously transferred to the low pressure side gas phase polymerization tank or the hopper for the post process
The polyolefin powder according to any one of claims 6 to 10, wherein the polyolefin powder is a homopolymer of ethylene or propylene, or two or more copolymers selected from ethylene, propylene, and 1-butene. Method.
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| WO2012175469A1 (en) | 2011-06-21 | 2012-12-27 | Basell Polyolefine Gmbh | Method and apparatus for discharging a polymer from a gas-phase reactor |
| CN106432551A (en) * | 2015-08-11 | 2017-02-22 | 中国石油化工股份有限公司 | Method and equipment for producing polypropylene through intermittent liquid phase bulk method |
| EP3450009A1 (en) | 2017-08-29 | 2019-03-06 | Sumitomo Chemical Company, Limited | Method for producing polyolefin |
| EP4302868A1 (en) | 2022-07-05 | 2024-01-10 | Sumitomo Chemical Company, Limited | Polyolefin production apparatus and polyolefin production method |
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| JPH093103A (en) * | 1995-02-24 | 1997-01-07 | Bp Chem Internatl Ltd | Apparatus and method for polymerizing olefin in gas phase |
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| JPH06100623A (en) * | 1992-06-18 | 1994-04-12 | Spherilene Srl | Method and apparatus for vapor phase polymerization of olefin |
| JPH093103A (en) * | 1995-02-24 | 1997-01-07 | Bp Chem Internatl Ltd | Apparatus and method for polymerizing olefin in gas phase |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2012175469A1 (en) | 2011-06-21 | 2012-12-27 | Basell Polyolefine Gmbh | Method and apparatus for discharging a polymer from a gas-phase reactor |
| CN103732634A (en) * | 2011-06-21 | 2014-04-16 | 巴塞尔聚烯烃股份有限公司 | Method and apparatus for discharging a polymer from a gas-phase reactor |
| US8853334B2 (en) | 2011-06-21 | 2014-10-07 | Basell Polyolefine Gmbh | Method and apparatus for discharging a polymer from a gas-phase reactor |
| CN106432551A (en) * | 2015-08-11 | 2017-02-22 | 中国石油化工股份有限公司 | Method and equipment for producing polypropylene through intermittent liquid phase bulk method |
| EP3450009A1 (en) | 2017-08-29 | 2019-03-06 | Sumitomo Chemical Company, Limited | Method for producing polyolefin |
| US10815315B2 (en) | 2017-08-29 | 2020-10-27 | Sumitomo Chemical Company, Limited | Method for producing polyolefin |
| EP4302868A1 (en) | 2022-07-05 | 2024-01-10 | Sumitomo Chemical Company, Limited | Polyolefin production apparatus and polyolefin production method |
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