JPH0618822B2 - Loop reactor for olefin polymerization - Google Patents
Loop reactor for olefin polymerizationInfo
- Publication number
- JPH0618822B2 JPH0618822B2 JP15207385A JP15207385A JPH0618822B2 JP H0618822 B2 JPH0618822 B2 JP H0618822B2 JP 15207385 A JP15207385 A JP 15207385A JP 15207385 A JP15207385 A JP 15207385A JP H0618822 B2 JPH0618822 B2 JP H0618822B2
- Authority
- JP
- Japan
- Prior art keywords
- valve
- pipe
- upward
- tube
- downward
- 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 - Lifetime
Links
- 238000006116 polymerization reaction Methods 0.000 title claims description 26
- 150000001336 alkenes Chemical class 0.000 title claims description 13
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims description 13
- 238000000605 extraction Methods 0.000 claims description 39
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 239000002002 slurry Substances 0.000 description 28
- 229920000642 polymer Polymers 0.000 description 12
- 239000002904 solvent Substances 0.000 description 8
- 239000000178 monomer Substances 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 239000003426 co-catalyst Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 230000007704 transition Effects 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- -1 comonomer Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000000977 initiatory effect Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1812—Tubular reactors
- B01J19/1837—Loop-type reactors
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Polymerisation Methods In General (AREA)
Description
【発明の詳細な説明】 ［産業上の利用分野］ この発明はオレフィン重合用ループ反応器に関し、さら
に詳しく言うと、スタートアップまでの時間の短縮およ
びスラリーの滞留時間の制御を可変することのできるオ
レフィン重合用ループ反応器に関する。Description: TECHNICAL FIELD The present invention relates to an olefin polymerization loop reactor, and more specifically, it is possible to shorten the time until start-up and control the residence time of slurry to be variable. It relates to a loop reactor for polymerization.
［従来の技術およびその問題点］ 従来、オレフィン重合用の反応器として用いられている
ループ反応器には、セットリングレグと称する下向き抜
出し管が設けられている（米国特許第３３７４２１１
号、米国特許第３３２４０９３号、米国特許第３２４２
１５０号参照）。[Prior Art and Problems Thereof] A loop reactor conventionally used as a reactor for olefin polymerization is provided with a downward extraction pipe called a set ring leg (US Pat. No. 3,374,211).
U.S. Pat. No. 3,324,093, U.S. Pat. No. 3,242.
150).
一般に、未反応モノマーのロスを防ぐために、反応器か
ら抜出すポリマーのスラリー濃度はできるだけ高くしな
ければならない。これに対し、ループ反応器内では、攪
拌器の保護および流動状態を一定に保持する必要性か
ら、反応器内のスラリー濃度はあまり高くすることがで
きない。したがって、下向き抜出し管付きループ反応器
では、反応器内のスラリー濃度を余り高くせずに一定に
しておき、下向き抜出し管でスラリー濃度を高めてか
ら、この下向き抜出し管からスラリーを取り出してい
る。Generally, the slurry concentration of polymer withdrawn from the reactor should be as high as possible to prevent loss of unreacted monomer. On the other hand, in the loop reactor, the slurry concentration in the reactor cannot be increased so much because it is necessary to protect the stirrer and keep the fluid state constant. Therefore, in the loop reactor with the downward extraction pipe, the slurry concentration in the reactor is kept constant without being made too high, the slurry concentration is increased by the downward extraction pipe, and then the slurry is taken out from the downward extraction pipe.
しかしながら、従来のこの下向き抜出し管付きループ反
応器には、次のような問題点がある。However, this conventional loop reactor with a downward extraction tube has the following problems.
スタートアップ時の問題点 ループ反応器は、終始、ループ反応管内に原料等を供給
する一方、供給量とほぼ同じ量を排出しなればならな
い。したがって、スタートアップ時に、供給量と同じ量
のポリマースラリーを下向き抜出し管から抜き出してし
まうと、折角、重合したポリマースラリーを抜き出して
しまうこととなり、定常状態に到達するまでに時間がか
かる。Problems at startup The loop reactor must supply raw materials and the like into the loop reaction tube from beginning to end, but must discharge almost the same amount as the supply amount. Therefore, at the time of startup, if the same amount of the polymer slurry as the supply amount is extracted from the downward extraction pipe, the polymerized polymer slurry will be extracted at all, and it takes time to reach a steady state.
定常運転時の問題点 スラリーの滞留時間の変更の必要性を生じたとき、複数
の下向き抜出し管を作動して運転中であれば、その中の
何本かの下向き抜出し管の作動を停止することで滞留時
間を長くすることができる。また、下向き抜出し管の作
動本数を増すことにより、滞留時間の短期化を図ること
ができる。しかしながら、一旦停止した下向き抜出し管
を再起動するときは、バルブに付着したパウダーにより
作動不良を起こし、滞留時間の変動を行なうことに問題
があった。Problems during steady operation When it becomes necessary to change the residence time of the slurry, if a plurality of downward discharge pipes are operating and they are in operation, the operation of some of the downward discharge pipes is stopped. Therefore, the residence time can be lengthened. In addition, the retention time can be shortened by increasing the number of operation of the downward extraction pipes. However, when restarting the downward extraction pipe that was once stopped, there was a problem in that the powder adhering to the valve caused a malfunction and the residence time was varied.
この発明は前記事情に基づいてなされたものである。The present invention has been made based on the above circumstances.
すなわち、この発明の目的は、前記問題点を解決し、ス
タートアップまでの時間を短縮すると共に管の閉塞事故
を生じることなくスラリーの滞留時間を自由に可変する
ことのできるループ反応器を提供することを目的とする
ものである。That is, an object of the present invention is to solve the above-mentioned problems, to provide a loop reactor capable of shortening the time until startup and freely varying the residence time of the slurry without causing a pipe clogging accident. The purpose is.
［前記目的を達成するための手段］ 前記目的を達成するためのこの発明の概要は、下向き抜
出し管を備えたループ反応管に、開閉バルブを有する上
向き抜出し管を設け、前記下向き抜出し管と前記ループ
反応管との間で、かつ前記ループ反応管の近傍に第１開
閉バルブを、前記第１開閉バルブの下方に第２開閉バル
ブをそれぞれ設けたことを特徴とするオレフィン重合用
ループ反応器である。[Means for Achieving the Object] The outline of the present invention for achieving the object is to provide a loop reaction tube having a downward extraction tube with an upward extraction tube having an opening / closing valve, and to provide the downward extraction tube and the A loop reactor for olefin polymerization, characterized in that a first opening / closing valve is provided between the loop reaction tube and in the vicinity of the loop reaction tube, and a second opening / closing valve is provided below the first opening / closing valve. is there.
さらに図面を参照しながら詳述すると、次のとおりであ
る。The details will be described below with reference to the drawings.
第１図はこの発明を示す説明図である。FIG. 1 is an explanatory view showing the present invention.
第１図に示すように、オレフィン重合用ループ反応器１
は、上昇管２、下降管３、上方および下方の水平移行管
４および５よりなる環状のループ反応管を備え、この下
方水平移行管４には、たとえば原料モノマー、コモノマ
ー、触媒、助触媒、溶媒、必要に応じて分子量調節剤等
を供給する導入管６，７を結合すると共に管内に攪拌機
８を備え、前記上昇管２および下降管３の外周には、管
内で発生する反応熱を除去するために、冷却媒体が循環
可能な冷却ジャケット９を備えている。また、上方また
は下方に位置する水平移行管４あるいは５には、複数の
たとえば３基の下向き抜出し管１０を備える。As shown in FIG. 1, loop reactor 1 for olefin polymerization
Comprises an annular loop reaction tube consisting of an ascending tube 2, a descending tube 3, and upper and lower horizontal transfer tubes 4 and 5, in which the lower horizontal transfer tube 4 comprises, for example, raw material monomer, comonomer, catalyst, cocatalyst, Introducing pipes 6 and 7 for supplying a solvent and a molecular weight adjusting agent, etc., if necessary, is equipped with a stirrer 8 in the pipes, and the heat of reaction generated in the pipes is removed on the outer periphery of the ascending pipe 2 and the descending pipe 3. In order to do so, a cooling jacket 9 through which a cooling medium can be circulated is provided. Further, the horizontal transition pipe 4 or 5 located above or below is provided with a plurality of, for example, three downward extraction pipes 10.
前記構成のオレフィン重合用ループ反応器１は、一般
に、導入管６，７から原料モノマー、触媒等を供給して
ループ反応管内を満液状態とし、攪拌機８によりループ
反応器内を３〜１０ｍ／秒程度の速度の乱流状態にして
前記原料モノマー等を循環する。循環中に原料モノマー
が重合してポリマースラリーとなり、重合により発生す
る熱は冷却ジャケット９により除去する。In the olefin polymerization loop reactor 1 having the above-described structure, generally, the raw material monomer, the catalyst, etc. are supplied from the introduction pipes 6 and 7 to fill the inside of the loop reaction pipe with a stirrer 8 and the inside of the loop reactor 3 to 10 m / m. The raw material monomers and the like are circulated in a turbulent state at a speed of about a second. During the circulation, the raw material monomers are polymerized into a polymer slurry, and the heat generated by the polymerization is removed by the cooling jacket 9.
この発明では、前記構成のオレフィン重合用ループ反応
器１における上方または下方の水平移行管４あるいは５
に、上向き抜出し管１１を配設し、ループ反応管内の溶
媒を抜き取ることができるようになっている。In the present invention, the upper or lower horizontal transfer pipe 4 or 5 in the olefin polymerization loop reactor 1 having the above-described configuration is used.
Further, an upward withdrawing tube 11 is provided so that the solvent in the loop reaction tube can be withdrawn.
この上向き抜出し管１１の「上向き」とは水平線より上
方に向く意であり、本来、この上向き抜出し管１１の上
向き角度（水平線に対する鋭角）αは、水平線に対して
０°を超えるものであれば良い。とは言っても、この発
明の効果を十分に奏するためには、この上向き抜出し管
１１の上向き角度αは、通常、１０°以上とし、特に３
５°以上とするのが好ましい。The "upward" of the upward extraction pipe 11 means upward from the horizontal line, and originally, the upward angle (the acute angle with respect to the horizontal line) α of the upward extraction pipe 11 is more than 0 ° with respect to the horizontal line. good. However, in order to sufficiently bring out the effect of the present invention, the upward angle α of the upward extraction pipe 11 is usually 10 ° or more, and particularly 3 °
It is preferably 5 ° or more.
この上向き抜出し管１１の配設本数には特に制限がな
い。There is no particular limitation on the number of the upward extraction pipes 11 arranged.
また、この上向き抜出し管１１の直径についても特に制
限がなく、通常は、ループ反応管の規模等により適宜に
決定するものである。Further, the diameter of the upward withdrawal pipe 11 is not particularly limited, and is usually appropriately determined depending on the scale of the loop reaction pipe and the like.
さらにこの上向き抜出し管１１には、言うまでもない
が、バルブ１２を設けていて、ループ反応管内の溶媒等
を抜き取るときにはこのバルブ１２を作動し、抜き取ら
ないときにはこのバルブ１２を閉状態にするようになっ
ている。Needless to say, the upward discharge pipe 11 is provided with a valve 12 so that the valve 12 is operated when the solvent or the like in the loop reaction pipe is extracted, and the valve 12 is closed when the solvent is not extracted. ing.
この上向き抜出し管１１を有してなるオレフィン重合用
ループ反応器１は、配設する下向き抜出し管１０の本数
に特に制限がないが、通常、１〜４本程度が適当であ
る。The olefin polymerization loop reactor 1 having the upward discharge pipe 11 has no particular limitation on the number of downward discharge pipes 10 to be provided, but normally 1 to 4 is suitable.
この発明では、この下向き抜出し管１０には、水平移行
管４，５の極く近傍に第１バルブ１３を設ける。また、
この第１バルブ１３よりもさらに下方に第２バルブ１４
を取り付けておく。第１バルブ１３を設け、閉状態にし
ておくと、下向き抜出し管１０内にポリマーが詰まって
閉塞することがなくなる。前記バルブ１２および第２バ
ルブ１４については、たとえばループ反応管内に圧力検
出手段を設けておき、この圧力検出手段から出力される
検出信号に基づき、中央制御手段により、これらバルブ
１２および第２バルブ１４の作動状態および閉状態を自
動制御可能に構成しておくのが好ましい。なお、バルブ
１２および第２バルブ１４の作動状態としては、ループ
反応管内の圧力調整のために、バルブ開閉を交互に瞬間
的にくりかえして行なうものである。In the present invention, the downward extraction pipe 10 is provided with the first valve 13 in the immediate vicinity of the horizontal transition pipes 4 and 5. Also,
The second valve 14 is provided below the first valve 13.
Attached. When the first valve 13 is provided and kept in the closed state, the downward extraction pipe 10 is prevented from being clogged with the polymer and blocked. Regarding the valve 12 and the second valve 14, for example, pressure detecting means is provided in the loop reaction tube, and based on the detection signal output from the pressure detecting means, the central control means controls the valve 12 and the second valve 14. It is preferable that the operating state and the closed state are automatically controllable. The operating states of the valve 12 and the second valve 14 are such that the valves are opened and closed alternately and repeatedly in order to adjust the pressure in the loop reaction tube.
［作用］ 次に以上構成の作用について説明する。[Operation] Next, the operation of the above configuration will be described.
このオレフィン重合用ループ反応器の運転を次のように
する。The operation of this olefin polymerization loop reactor is as follows.
導入管６，７から原料モノマー等をループ反応管に満液
状態で供給する。攪拌器８でループ反応管内に原料モノ
マー等を循環する。また、重合開始後に発生する重合熱
を除去するために、冷却ジャケット９内に冷却媒体を循
環する。なお、第１バルブ１３は閉状態とし、第２バル
ブ１４は作動させず、バルブ１２を作動状態にしてお
く。Raw material monomers and the like are supplied from the introduction pipes 6 and 7 to the loop reaction pipe in a liquid-filled state. The raw material monomer and the like are circulated in the loop reaction tube by the stirrer 8. Further, a cooling medium is circulated in the cooling jacket 9 in order to remove the polymerization heat generated after the initiation of the polymerization. The first valve 13 is closed, the second valve 14 is not operated, and the valve 12 is operated.
次いで、導入管６または７から触媒、助触媒等をループ
反応管内に導入する。ループ反応管内で直ちに重合反応
がスタートする。重合反応の進行と共にループ反応管内
の液は、スラリーとなっていく。スラリー濃度が目標値
に達するまで、バルブ１２を作動状態にしたままループ
反応管内でスラリーを循環すると、上向き抜出管１１か
らは溶媒が排出されて行く。このように上向き抜出し管
１１から溶媒を抜出し、ポリマーを排出しないので、ル
ープ反応管内では、スラリー濃度が急速に高まっていく
こととなる。Then, a catalyst, a co-catalyst, etc. are introduced into the loop reaction tube from the introduction tube 6 or 7. The polymerization reaction starts immediately in the loop reaction tube. As the polymerization reaction progresses, the liquid in the loop reaction tube becomes a slurry. When the slurry is circulated in the loop reaction tube with the valve 12 kept in the operating state until the slurry concentration reaches the target value, the solvent is discharged from the upward extraction tube 11. In this way, the solvent is extracted from the upward extraction tube 11 and the polymer is not discharged, so that the slurry concentration is rapidly increased in the loop reaction tube.
スラリー濃度が所定値に達して定常状態となったなら
ば、第１バルブ１３を開状態にする。そうすると、下向
き抜出し管１０における第２バルブ１４までの部分にス
ラリーが侵入し、この部分でポリマーの沈降により、濃
縮されたポリマースラリーとなる。次いで、前記バルブ
１２を閉状態にすると共に第２バルブ１４を作動状態に
する。ポリマースラリーは、この下向き抜出し管１０か
ら排出される。なお、第１バルブ１３は水平移行管５の
極く近傍に配設しているので、水平移行管５から第１バ
ルブ１３までの間にポリマーが沈積することによる管閉
塞事故のおこる心配がない。When the slurry concentration reaches a predetermined value and reaches a steady state, the first valve 13 is opened. Then, the slurry penetrates into the portion of the downward extraction pipe 10 up to the second valve 14, and the polymer is precipitated in this portion to become a concentrated polymer slurry. Next, the valve 12 is closed and the second valve 14 is activated. The polymer slurry is discharged from the downward discharge pipe 10. Since the first valve 13 is arranged very close to the horizontal transfer pipe 5, there is no fear of causing a pipe blockage accident due to polymer deposition between the horizontal transfer pipe 5 and the first valve 13. .
なお、定常状態に達した後に、ループ反応管内でのスラ
リーの滞留時間を長期化するときは、閉状態としていた
上向き抜出し管を作動状態にすれば良く、これとは逆に
滞留時間を短期化するときには、上向き抜出し管の作動
を止めるか、または下向き抜出し管の作動本数を増加す
れば良い。In addition, when the retention time of the slurry in the loop reaction tube is prolonged after reaching the steady state, it is sufficient to activate the upward extraction tube that was closed, and conversely, the retention time is shortened. At this time, the operation of the upward extraction pipe may be stopped or the number of downward extraction pipes may be increased.
［実施例］ 次にこの発明の実施例を示す。なお、この発明はこの実
施例に限定されるものではないことは言うまでもない。[Embodiment] Next, an embodiment of the present invention will be described. Needless to say, the present invention is not limited to this embodiment.
第１図において、内径１５０ｍｍおよび内容積３７０
のループ反応器の上方水平移行管５に、内径38.4ｍｍお
よび長さ１ｍの寸法を有する３本の下向き抜出し管１０
と、内径25.0ｍｍおよび長さ0.4ｍの寸法を有する３本
の上向き抜出し管１１と、1/4インチのバルブ１２、第
１バルブ１３および第２バルブ１４と、導入管６，７と
攪拌器８と、冷却ジャケット９とを備えたオレフィン重
合用ループ反応器を使用した。なお、前記上向き抜出し
管１１の上向き角度は９０°である。In FIG. 1, the inner diameter is 150 mm and the inner volume is 370.
In the upper horizontal transfer tube 5 of the loop reactor of No. 3, with three downward extraction tubes 10 having an inner diameter of 38.4 mm and a length of 1 m.
And three upward extraction tubes 11 having an inner diameter of 25.0 mm and a length of 0.4 m, a 1/4 inch valve 12, a first valve 13 and a second valve 14, introduction tubes 6, 7 and a stirrer. A loop reactor for olefin polymerization equipped with 8 and a cooling jacket 9 was used. The upward angle of the upward extraction pipe 11 is 90 °.
そして、第２バルブ１４の作動時間を0.9秒、バルブ１
２の作動時間を0.7秒とし、プロピレンをそれぞれ導入
管からループ反応管内に供給すると共に、重合温度７０
℃、圧力３６Ｋｇ／cm2Ｇ、重合時間２時間で５０Ｋｇ
のポリプロピレンが生産可能となるように、所定の触媒
量および助触媒比で触媒および助触媒を溶媒であるヘプ
タン１０Ｋｇ／時間とともに導入管７よりループ反応管
内に供給して、次のような実験を行なった。結果を第１
表に示す。Then, the operation time of the second valve 14 is 0.9 seconds, the valve 1
The operating time of 2 was set to 0.7 seconds, and propylene was supplied into the loop reaction tube from each of the introduction tubes and the polymerization temperature was adjusted to 70
℃, pressure 36Kg / cm 2 G, polymerization time 2 hours 50Kg
In order to make it possible to produce polypropylene, the catalyst and the co-catalyst are supplied at a predetermined catalyst amount and a co-catalyst ratio from the introduction pipe 7 into the loop reaction pipe together with 10 Kg / hour of the solvent heptane, and the following experiment is conducted. I did. First result
Shown in the table.
（実験例１〜３、比較実験例１〜３） 第１表に示すスタート方法により、第１表に示すプロピ
レンの供給量で重合反応を行なった。(Experimental Examples 1 to 3, Comparative Experimental Examples 1 to 3) By the starting method shown in Table 1, the polymerization reaction was carried out with the supply amount of propylene shown in Table 1.
スラリー濃度が目標値に達するまでの時間、定常状態と
なったときのスラリー濃度、および定常状態に達するま
での時間を第１表に示す。Table 1 shows the time until the slurry concentration reaches the target value, the slurry concentration at the steady state, and the time until the steady state is reached.
（比較実験例４） 比較実験例２と同様にして重合反応をスタートし、定常
状態となった後、滞留時間を長期化するために１本の下
向き抜出し管の第２バルブを閉とし、つまり、２本の下
向き抜出し管から１本の下向き抜出し管にすることによ
りスラリー密度を６１０Ｋｇ／m3までに高めた。１８時
間後に、停止していた下向き抜出し管の第２バルブを再
び開状態としたが、第２バルブが作動不良となり使用不
能となった。 (Comparative Experimental Example 4) The polymerization reaction was started in the same manner as in Comparative Experimental Example 2, and after reaching a steady state, the second valve of one downward extraction pipe was closed to prolong the residence time, that is, The slurry density was increased to 610 Kg / m 3 by changing from two downward discharge pipes to one downward discharge pipe. After 18 hours, the second valve of the downward discharge pipe that had been stopped was opened again, but the second valve failed to operate and became unusable.
（実験例４） 実験例１と同様の方法で重合反応を開始し、定常運転と
なった後、滞留時間を長期化するために１本の上向き抜
出し管のバルブを作動状態にし、つまり、２本の下向き
抜出し管による定常運転から１本の上向き抜出し管と２
本の下向き抜出し管とによる定常運転をすることにより
スラリー密度を６１０Ｋｇ／m3にまで高めることができ
た。(Experimental Example 4) After the polymerization reaction was started in the same manner as in Experimental Example 1 and the steady operation was performed, one valve of the upward withdrawing pipe was activated to prolong the residence time, that is, 2 From the normal operation with two downward extraction pipes, one upward extraction pipe and two
It was possible to raise the slurry density to 610 Kg / m 3 by performing steady operation with the downward discharge tube of the book.
４８時間後、１本の上向き抜出し管を閉状態にして運転
すると、スラリー密度は再び５８８Ｋｇ／m3となった。After 48 hours, when operating with one upward extraction tube closed, the slurry density was again 588 Kg / m 3 .
［発明の効果］ 以上に詳述したように、この発明によると、下向き抜出
し管を備えたループ反応器に上向き抜出し管を設けたの
で、重合スタート時には、下向き抜出し管を閉状態と
し、上向き抜出し管を作動状態とすることにより、折角
重合したポリマースラリーを無駄にすることなく、溶媒
を除去することができて、これによって所定のスラリー
濃度に迅速に達成することができる。しかも、定常運転
に達した後には、下向き抜出し管を止めずに上向き抜出
し管の作動本数を調節することによりポリマースラリー
の滞留時間を長短自由に制御することができる。[Effects of the Invention] As described in detail above, according to the present invention, since the upward withdrawal tube is provided in the loop reactor equipped with the downward withdrawal tube, the downward withdrawal tube is closed at the start of polymerization, and the upward withdrawal tube is withdrawn. By activating the tube, the solvent can be removed without wasting the polymer slurry that has been polymerized in the corner, thereby achieving the desired slurry concentration quickly. Moreover, after the steady operation is reached, the residence time of the polymer slurry can be freely controlled by adjusting the number of operating upward pull-out pipes without stopping the downward pull-out pipes.
この発明によると、前述の重合開始後定常状態に達する
までの時間の短縮および滞留時間の制御を、上向き抜出
し管を設置するとの簡単な構成で達成することができ
る。According to the present invention, the shortening of the time until the steady state is reached after the initiation of the polymerization and the control of the residence time can be achieved with a simple configuration in which an upward extraction pipe is installed.
第１図はこの発明の構成を示す概略説明図および第２図
は水平移行管に上向き抜出し管と下向き抜出し管とを配
設した状態を示す一部切欠断面図である。 １……オレフィン重合用ループ反応器、１０……下向き
抜出し管、１１……上向き抜出し管、１３……第１バル
ブ。FIG. 1 is a schematic explanatory view showing the configuration of the present invention, and FIG. 2 is a partially cutaway sectional view showing a state in which an upward extraction pipe and a downward extraction pipe are arranged in a horizontal transition pipe. 1 ... Olefin polymerization loop reactor, 10 ... Downward extraction tube, 11 ... Upward extraction tube, 13 ... First valve.
Claims (2)
開閉バルブを有する上向き抜出し管を設け、前記下向き
抜出し管と前記ループ反応管との間で、かつ前記ループ
反応管の近傍に第１開閉バルブを、前記第１開閉バルブ
の下方に第２開閉バルブをそれぞれ設けたことを特徴と
するオレフィン重合用ループ反応器。1. A loop reaction tube having a downward extraction tube,
An upward extraction pipe having an opening / closing valve is provided, and a first opening / closing valve is provided between the downward extraction pipe and the loop reaction pipe and in the vicinity of the loop reaction pipe, and a second opening / closing valve is provided below the first opening / closing valve. A loop reactor for olefin polymerization, each of which is provided with.
向に対して１０°以上である前記特許請求の範囲第１項
に記載のオレフィン重合用ループ反応器。2. The loop reactor for olefin polymerization according to claim 1, wherein the upward angle of the upward discharge tube is 10 ° or more with respect to the horizontal direction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15207385A JPH0618822B2 (en) | 1985-07-10 | 1985-07-10 | Loop reactor for olefin polymerization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15207385A JPH0618822B2 (en) | 1985-07-10 | 1985-07-10 | Loop reactor for olefin polymerization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6213408A JPS6213408A (en) | 1987-01-22 |
| JPH0618822B2 true JPH0618822B2 (en) | 1994-03-16 |
Family
ID=15532461
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15207385A Expired - Lifetime JPH0618822B2 (en) | 1985-07-10 | 1985-07-10 | Loop reactor for olefin polymerization |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0618822B2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100531628B1 (en) | 1998-03-20 | 2005-11-29 | 엑손모빌 케미칼 패턴츠 인코포레이티드 | Continuous slurry polymerization volatile removal |
| US6281300B1 (en) | 1998-03-20 | 2001-08-28 | Exxon Chemical Patents, Inc. | Continuous slurry polymerization volatile removal |
| US20020111441A1 (en) | 1998-03-20 | 2002-08-15 | Kendrick James Austin | Continuous slurry polymerization volatile removal |
| US7268194B2 (en) | 1998-03-20 | 2007-09-11 | Exxonmobil Chemical Patents Inc. | Continuous slurry polymerization process and apparatus |
| AU2002238109B2 (en) * | 2002-02-19 | 2007-12-06 | Chevron Phillips Chemical Company Lp | Continuous slurry polymerization process and apparatus |
| ES2462166T3 (en) * | 2011-12-19 | 2014-05-22 | Borealis Ag | Loop reactor that provides advanced control of production division |
| US10029230B1 (en) | 2017-01-24 | 2018-07-24 | Chevron Phillips Chemical Company Lp | Flow in a slurry loop reactor |
-
1985
- 1985-07-10 JP JP15207385A patent/JPH0618822B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6213408A (en) | 1987-01-22 |
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