JPH0349925A - Devolatile extrusion method of thermoplastic polymer composition - Google Patents
Devolatile extrusion method of thermoplastic polymer compositionInfo
- Publication number
- JPH0349925A JPH0349925A JP1185631A JP18563189A JPH0349925A JP H0349925 A JPH0349925 A JP H0349925A JP 1185631 A JP1185631 A JP 1185631A JP 18563189 A JP18563189 A JP 18563189A JP H0349925 A JPH0349925 A JP H0349925A
- Authority
- JP
- Japan
- Prior art keywords
- polymer composition
- volatile
- screw
- polymer
- cylinder
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000000203 mixture Substances 0.000 title claims abstract description 59
- 229920001169 thermoplastic Polymers 0.000 title claims abstract description 12
- 238000001125 extrusion Methods 0.000 title abstract 4
- 229920000642 polymer Polymers 0.000 claims abstract description 59
- 238000000034 method Methods 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 239000007787 solid Substances 0.000 claims abstract description 4
- 239000000178 monomer Substances 0.000 claims description 10
- 239000002904 solvent Substances 0.000 claims description 7
- 239000006227 byproduct Substances 0.000 claims description 6
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 238000013459 approach Methods 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 4
- 238000012662 bulk polymerization Methods 0.000 description 4
- 238000010528 free radical solution polymerization reaction Methods 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- BHIWKHZACMWKOJ-UHFFFAOYSA-N methyl isobutyrate Chemical compound COC(=O)C(C)C BHIWKHZACMWKOJ-UHFFFAOYSA-N 0.000 description 2
- 230000000379 polymerizing effect Effects 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 229920002554 vinyl polymer Polymers 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000001252 acrylic acid derivatives Chemical class 0.000 description 1
- 150000004996 alkyl benzenes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229920001519 homopolymer Polymers 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- WDAXFOBOLVPGLV-UHFFFAOYSA-N isobutyric acid ethyl ester Natural products CCOC(=O)C(C)C WDAXFOBOLVPGLV-UHFFFAOYSA-N 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- -1 vinyl compound Chemical class 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 239000003039 volatile agent Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/76—Venting, drying means; Degassing means
- B29C48/765—Venting, drying means; Degassing means in the extruder apparatus
- B29C48/766—Venting, drying means; Degassing means in the extruder apparatus in screw extruders
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/395—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders
- B29C48/397—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders using a single screw
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
Abstract
Description
【発明の詳細な説明】
〈産業上の利用分野〉
本発明は、溶液重合法あるいは塊状重合法によって得ら
れた未反応単量体、溶剤、揮発性、副生成物あるいは不
純物等の揮発成分を含有する熱可塑性重合体組成物から
、これらの揮発成分を連続的に分離する方法に関する。[Detailed Description of the Invention] <Industrial Application Field> The present invention is directed to removing volatile components such as unreacted monomers, solvents, volatiles, by-products, and impurities obtained by solution polymerization or bulk polymerization. The present invention relates to a method for continuously separating these volatile components from a thermoplastic polymer composition containing them.
〈従来の技術）
溶液重合法、塊状重合法で得られた揮発成分を含む流動
状の重合体組成物をスクリュー式脱揮押出機に供給し、
揮発分を除去し、重合体を取り出す方法は、例えば特公
昭５１−２９９１４号公報、特公昭５２−１７５５５号
公報、特開昭５７〜４９６０３号公報、特開昭５８−１
４７３３２号公報など、これまでに種々のＩｌ案がある
。(Prior art) A fluid polymer composition containing volatile components obtained by a solution polymerization method or a bulk polymerization method is supplied to a screw type devolatilizing extruder,
Methods for removing volatile components and extracting the polymer are described, for example, in Japanese Patent Publication No. 51-29914, Japanese Patent Publication No. 17555-1982, Japanese Patent Application Laid-open No. 57-49603, and Japanese Patent Application Laid-open No. 58-1.
There have been various Il proposals such as No. 47332.
これらの方法は、加圧昇温された重合体組成物を、減圧
下、あるいは加圧下のスクリューに細孔部を用い、直接
吹き付ける方法である。These methods are methods in which a polymer composition heated under pressure is directly sprayed onto a screw under reduced pressure or under pressure using a pore section.
〈発明が解決しようとする課題）
従来方法では重合体組成物をスクリューに直接吹き付け
、その部分で一時的に揮発成分が気化するので、揮発成
分の出口の方に重合体が同伴して出て行き易い。(Problem to be solved by the invention) In the conventional method, the polymer composition is directly sprayed onto the screw, and the volatile components are temporarily vaporized at that part, so the polymer is accompanied by the volatile components and comes out toward the outlet. Easy to get to.
揮発成分出口と、重合体組成物の供給口を同一の部分、
スクリューをはさんで逆の方向、あるいはある程度の距
離を設けているものなど、従来の方法では提案があるも
のの、揮発成分に同伴して、重合体が飛び出して行くこ
とを抑制するには、未だ改良の余地がある。The volatile component outlet and the polymer composition supply port are in the same part,
Although there are proposals for conventional methods such as using screws in opposite directions or at a certain distance, there is still no way to prevent the polymer from flying out along with the volatile components. There is room for improvement.
また、細孔部を用いてスクリューに直接吹き付けるので
装置上も複雑なものとなる。Furthermore, since the spray is directly sprayed onto the screw using the pores, the equipment becomes complicated.
く課題を解決するための手段〉
本発明は、未反応単量体、溶剤及び／または揮発性副生
物を含有する熱可塑性重合体組成物をスクリュー式脱揮
押出機をもちいて、これらの揮発成分を分離するに当り
、該スクリュー式脱揮押出機がスクリューの軸方向に駆
動部側から先端部側に向って揮発成分出口、重合体組成
物供給口、脱揮済み重合体出口の順に配列したものであ
り、該重合体組成物にあらかじめ揮発成分の揮発に必要
な熱量の一部または全部を与え、気−液混合流あるいは
気−液一固混合流の状態で、重合体組成物供給口に供給
し、揮発成分をシリンダーとスクリューで形成される空
間中を、５０ｍ／秒以下の流速で通過させて揮発成分出
口から取り出すことを特徴とする熱可塑性重合体組成物
の脱揮方法である。Means for Solving the Problems> The present invention uses a screw type devolatilizing extruder to evaporate a thermoplastic polymer composition containing unreacted monomers, solvents and/or volatile by-products. In separating the components, the screw type devolatilizing extruder is arranged in the axial direction of the screw from the drive part side to the tip end side in the order of volatile component outlet, polymer composition supply port, and devolatilized polymer outlet. The polymer composition is supplied in the form of a gas-liquid mixed flow or a gas-liquid-solid mixed flow by giving part or all of the heat necessary for volatilization of volatile components to the polymer composition in advance. A method for devolatilizing a thermoplastic polymer composition, characterized in that the volatile components are passed through a space formed by a cylinder and a screw at a flow rate of 50 m/sec or less and taken out from an outlet of the volatile components. be.
本発明の方法を適用する熱可塑性重合体組成物としては
、未反応単重体、溶剤及び／または揮発性副生成物など
の揮発成分を含むアルキル（メタ）アクリレート類、ス
チレン、ブタジェン、イソプロピレン等のビニル化合物
の単独重合体、または共重合体よりなる組成物であって
、塊状重合または溶液重合によって製造されたものであ
る。Thermoplastic polymer compositions to which the method of the present invention is applied include alkyl (meth)acrylates, styrene, butadiene, isopropylene, etc. containing volatile components such as unreacted monomers, solvents and/or volatile by-products. A composition consisting of a homopolymer or copolymer of a vinyl compound produced by bulk polymerization or solution polymerization.
本発明の方法でいう未反応単量体とは、上記ビニル単量
体を重合あるいは共重合させた後、重合体組成物中に存
在する重合してない残存単量体である。The unreacted monomer as used in the method of the present invention refers to unpolymerized residual monomers present in the polymer composition after polymerizing or copolymerizing the above-mentioned vinyl monomers.
また本発明の方法でいう重合体組成物中の溶剤とは、一
般に溶液重合として使用できる溶剤であれば特に限定し
ないが、溶剤の沸点が５５〜２５０℃の範囲にあるベン
ゼン、トルエン、キシレン、エチルベンゼン、クメン等
のアルキルベンゼン、メチルエチルケトン、メチルイソ
ブチレート、酢酸エチル等の有８ｇ溶剤である。In addition, the solvent in the polymer composition as used in the method of the present invention is not particularly limited as long as it can be generally used for solution polymerization, but includes benzene, toluene, xylene, etc. whose boiling point is in the range of 55 to 250°C. 8g of solvents include alkylbenzenes such as ethylbenzene and cumene, methyl ethyl ketone, methyl isobutyrate, and ethyl acetate.
また重合体組成物中の副生成物は、反応中に生成する揮
発性の低分子量物あるいは原料に含まれる揮発性の成分
である。By-products in the polymer composition are volatile low molecular weight substances produced during the reaction or volatile components contained in the raw materials.
なかでも熱可塑性重合体組成物としては、揮発成分が２
０〜７０重量％のメタクリル酸メチル系重合体組成物が
好適である。Among them, the thermoplastic polymer composition contains 2 volatile components.
A methyl methacrylate polymer composition of 0 to 70% by weight is preferred.
本発明の方法に適合するスクリュー式脱揮押出機の一例
の正面断面図を第１図に示す。FIG. 1 shows a front sectional view of an example of a screw type devolatilizing extruder suitable for the method of the present invention.
該脱揮押出機は一軸もしくはそれ以上の軸を持つ脱揮押
出機のいずれでも有効に使用できる。The devolatilizing extruder can be effectively used with any devolatilizing extruder having one or more shafts.
該脱揮押出機は、駆動部側から先端部側に向って、揮発
成分出口（以下、リアーベントと称する）、重合体組成
物供給口、脱揮済み重合体出口、の順に配列したもので
ある。The devolatilizing extruder has a volatile component outlet (hereinafter referred to as a rear vent), a polymer composition supply port, and a devolatilized polymer outlet arranged in this order from the drive section side to the tip side. .
また、脱揮済み重合体に残留する揮発成分をより少なく
するため必要に応じ、重合体組成物供給口と脱揮済み重
合体出口の間に、１つまたはそれ以上の揮発成分出口（
以下、フォアベントと称す）を設置してよい。In addition, in order to further reduce the volatile components remaining in the devolatilized polymer, one or more volatile component outlets (
(hereinafter referred to as a forevent) may be installed.
揮発成分を含有する熱可塑性重合体組成物にあらかじめ
、連発成分の揮発に必要な熱量の一部または全部を与え
るため加熱する。The thermoplastic polymer composition containing volatile components is heated in advance to provide part or all of the amount of heat necessary for volatilization of the volatile components.
この加熱は周知の方法でよく、該重合体組成物から該脱
揮押出機までの輸送の間、連続的に行うこともできる。This heating may be performed by a well-known method, and may be performed continuously during transportation from the polymer composition to the devolatilizing extruder.
加熱は、該重合体組成物が１５０〜２８０℃程度になる
までであり、この温度で気化が起らぬ様、加圧状態で行
う。Heating is carried out until the temperature of the polymer composition reaches approximately 150 to 280°C, and is carried out under pressure so that vaporization does not occur at this temperature.
該脱揮押出機の該重合体組成物供給口は、シリンダー径
に応じた大きさの開口であり該供給口に近づくにつれて
、揮発成分の一部は気化して、気体と液体の混合流、あ
るいは気体と液体と固体の混合流となり、該脱揮押出機
のシリンダーの中に入って行く。The polymer composition supply port of the devolatilizing extruder is an opening whose size corresponds to the diameter of the cylinder, and as it approaches the supply port, a portion of the volatile components are vaporized, resulting in a mixed flow of gas and liquid. Alternatively, it becomes a mixed stream of gas, liquid, and solid and enters the cylinder of the devolatilizing extruder.
既に揮発した成分、及びここで揮発した成分は、シリン
ダーとスクリューで形成される空間を通って、リアーベ
ントから出て行く。The components already volatilized and the components volatilized here pass through the space formed by the cylinder and screw and exit from the rear vent.
この空間を通る気体の揮発成分の流速を、５０＋ｍ／秒
以下にする。The flow rate of the volatile components of the gas through this space is 50+ m/sec or less.
流速がこれを越えるとリアーベントから重合体が同伴す
るので好ましくない。If the flow rate exceeds this, the polymer will be entrained from the rear vent, which is not preferable.
シリンダーとスクリューで形成される空間を揮発した成
分が流れる流速は、供給される該重合体組成物中の揮発
成分の量と、あらかじめ付与されていた熱量、及び重合
体組成物供給口付近から供給される熱量、及びシリンダ
ー内の圧力によって容易に調節することができる。The flow rate at which the volatile components flow through the space formed by the cylinder and screw depends on the amount of volatile components in the supplied polymer composition, the amount of heat applied in advance, and the supply from the vicinity of the polymer composition supply port. It can be easily adjusted by the amount of heat applied and the pressure inside the cylinder.
リアーベントの圧力は、５０〜１５００ｗＨｇである。The rear vent pressure is 50-1500 wHg.
この圧力が、あまり低いと、気化した揮発成分の体積が
大きくなり、シリンダーとスクリューで形成される空間
中のガス流速が高くなり、抜き出す揮発成分に同伴する
重合体が多くなり逆に圧力があまり高いと揮発成分が分
離しにくくなる。If this pressure is too low, the volume of the vaporized volatile components will increase, the gas flow rate in the space formed by the cylinder and screw will increase, and the amount of polymer accompanying the volatile components to be extracted will increase, conversely, the pressure will become too high. If the temperature is high, it becomes difficult to separate volatile components.
また、重合体組成物供給口とリアーベントとの軸方向距
離は長い程、重合体の同伴がしにくい。Furthermore, the longer the axial distance between the polymer composition supply port and the rear vent, the more difficult it is for the polymer to be entrained.
従って、この距離は、スクリュー径をＤとした時、３Ｄ
以上有ることが望ましい。Therefore, this distance is 3D when the screw diameter is D.
It is desirable to have at least the following.
ここで、未揮発の残留揮発成分を重合体出口の方向に順
次送りながらシリンダーから熱の供給し、揮発させてフ
ォアベントから抜き出す。Here, heat is supplied from the cylinder while sequentially sending the unvolatilized residual volatile components toward the polymer outlet, volatilizes them, and extracts them from the fore vent.
フォアベントの出口圧力は５〜１００ｍＨｇ程度である
。The outlet pressure of the fore vent is approximately 5 to 100 mHg.
この様にして、揮発成分が除かれた重合体を得ることが
できる。In this way, a polymer free of volatile components can be obtained.
リアーベント、フォアベントから抜き出された揮発成分
は、加圧冷却して液化させ回収することも可能である。The volatile components extracted from the rear vent and fore vent can also be liquefied and recovered by cooling under pressure.
〈発明の効果〉
揮発成分を含む熱可塑性重合体組成物を、スクリュー式
脱揮押出機により、揮発成分を分離除去する方法におい
て、特殊な装置を用いずとも分離効果が大きく、しかも
揮発成分出口から重合体の同伴を防止し得る。<Effects of the Invention> In a method for separating and removing volatile components from a thermoplastic polymer composition containing volatile components using a screw type devolatilizing extruder, the separation effect is large without using special equipment, and the volatile component exit Entrainment of polymers can be prevented from occurring.
しかも、得られる重合体に残留する揮発成分量を非常に
少くすることができる。Moreover, the amount of volatile components remaining in the resulting polymer can be extremely reduced.
〈実施例〉
使用するスクリュー式脱揮機は、第１図に示す概念を有
したものである。<Example> The screw type devolatilizer used has the concept shown in FIG.
実施例１〜３、比較例１
スクリュー式脱揮押出機は、田辺プラスチック■製単軸
押出機でその構造は；
・スクリュー径 Ｄ ５０鶴
・シリンダーの長さＬ １５００鶴
・リアーベントから重合体組成物供給口の間の距＃ １
５０鶴
・フォアベントの数 ２
・ スクリューとシリンダーの空間断面積 １０００
＋ｌｌ１）”運転条件は；
・リアーベントの出口圧力 第１表に示す。Examples 1 to 3, Comparative Example 1 The screw type devolatilizing extruder is a single-screw extruder manufactured by Tanabe Plastic ■, and its structure is as follows: - Screw diameter D 50 Tsuru - Cylinder length L 1500 Tsuru - Polymer composition from rear vent Distance between supply ports #1
50 Tsuru・Number of fore vents 2 ・Spatial cross-sectional area of screw and cylinder 1000
＋ll1)" Operating conditions are; - Rear vent outlet pressure is shown in Table 1.
・フォアベントから重合体組成物供給口までの平均シリ
ンダー温度 ２３５℃
・重合体組成物供給口から、重合体出口部までの平均シ
リンダー温度 ２１５℃
・フォアベントの出口圧力 平均 １５ｔｍｌ（ｇであ
る。- Average cylinder temperature from the fore vent to the polymer composition supply port: 235°C - Average cylinder temperature from the polymer composition supply port to the polymer outlet: 215°C - Fore vent outlet pressure: Average 15 tml (g).
重合体組成物として、メタクリル酸メチル９４重量％、
及びアクリル酸メチル６重量％からなる単量体混合物を
塊状重合して、得られた重合体含量６５重量％の組成物
を用い、これを、１５気圧に加圧下、２００℃まで加熱
し、第１表に示す量を、スクリュー式脱揮押出機に供給
し１２時間連続運転した。As a polymer composition, 94% by weight of methyl methacrylate,
A monomer mixture consisting of methyl acrylate and 6% by weight of methyl acrylate was subjected to bulk polymerization, and the resulting composition had a polymer content of 65% by weight. This was heated to 200° C. under a pressure of 15 atm. The amounts shown in Table 1 were supplied to a screw type devolatilizing extruder and operated continuously for 12 hours.
シリンダー内のガス流速、リアーベントから出る揮発成
分中の重合体の同伴量、得られる重合体中の残留揮発成
分含有量を第１表に示す。Table 1 shows the gas flow rate in the cylinder, the amount of polymer entrained in the volatile components exiting from the rear vent, and the residual volatile component content in the resulting polymer.
実施例４〜６、比較例２
スクリュー式脱揮押出機は、−日本製鋼所説の二軸押出
機ＴＥＸ−３０でその構造は；・スクリュー径 Ｄ
３０鶴
・シリンダーの長さＬ １２００鶴
・リアーベントから重合体組成物供給口の間の距離 １
２０訪
・フォアベントの数 ３
・ スクリューとシリンダーの空間断面積 ７００ｍ
ｍ”運転条件は；
・リアーベントの出口圧力 第１表にしめす。Examples 4 to 6, Comparative Example 2 The screw type devolatilizing extruder is a twin-screw extruder TEX-30 described by Japan Steel Works, and its structure is; - Screw diameter D
30 Tsuru・Cylinder length L 1200 Tsuru・Distance between rear vent and polymer composition supply port 1
20 visits・Number of fore vents 3・Spatial cross-sectional area of screw and cylinder 700m
The operating conditions are: - Rear vent outlet pressure is shown in Table 1.
・フォアベントから重合体組成物供給口までの平均シリ
ンダー温度 ２３５℃
・重合体組成物供給口から、重合体出口部までの平均シ
リンダー温度 ２１５℃
・フォアベントの出口圧力 平均 １５ｍＨｇである。- Average cylinder temperature from the fore vent to the polymer composition supply port: 235°C - Average cylinder temperature from the polymer composition supply port to the polymer outlet: 215°C - Fore vent outlet pressure: 15 mHg on average.
重合体組成物として、 メタクリル酸メチル９７重量％
、及びアクリル酸エチル３重量％からなる単量体混合物
を塊状重合して得られた重合体含量４０重量％の組成物
を用い、２５気圧に加圧下、２３０℃まで加熱し、第２
表に示す量を１２時間連続して、スクリュー式脱揮押出
機に供給し運転した。As a polymer composition, 97% by weight of methyl methacrylate
A composition having a polymer content of 40% by weight obtained by bulk polymerizing a monomer mixture consisting of
The amount shown in the table was continuously supplied to a screw type devolatilizing extruder for 12 hours, and the extruder was operated.
シリンダー内のガス流速、リアーベントから出る揮発成
分中の重合体の同伴量、得られる重合体中の残留揮発成
分含有量を第２表に示す。Table 2 shows the gas flow rate in the cylinder, the amount of polymer entrained in the volatile components exiting from the rear vent, and the residual volatile component content in the resulting polymer.
第２表Table 2
第１図は、本発明を実施するに適するスクリュー式脱揮
押出機の概念の正面断面図を示す。
第１図において、
ｌは、重合体組成物入口
２は、り剣々ント ３は、フォアベント４は、脱
揮済み重合体の出口
５は、スクリュ−６は、シリンダー
７は、軸封軸受は部 ８は、回転軸を示す。
第
図FIG. 1 shows a conceptual front sectional view of a screw type devolatilizing extruder suitable for carrying out the present invention. In FIG. 1, 1 is a polymer composition inlet 2, a cylinder 3 is a fore vent 4 is a devolatilized polymer outlet 5, a screw 6 is a cylinder 7 is a shaft sealing bearing Part 8 indicates the rotation axis. Diagram
Claims (4)
含有する熱可塑性重合体組成物をスクリュー式脱揮押出
機をもちいて、これらの揮発成分を分離するに当り、該
スクリュー式脱揮押出機が、スクリューの軸方向に駆動
部側から先端部側に向って、揮発成分出口、重合体組成
物供給口、脱揮済み重合体出口の順に配列したものであ
り、該重合体組成物にあらかじめ揮発成分の揮発に必要
な熱量の一部または全部を与え、気−液混合流あるいは
気−液−固混合流の状態で、重合体組成物供給口に供給
し、揮発した成分をシリンダーとスクリューで形成され
る空間中を５０ｍ／秒以下の流速で通過させて揮発成分
出口から取り出すことを特徴とする熱可塑性重合体組成
物の脱揮方法。(1) When a thermoplastic polymer composition containing unreacted monomers, solvents and/or volatile by-products is separated from these volatile components using a screw type devolatilizing extruder, the screw type devolatilizing extruder The devolatilizing extruder has a volatile component outlet, a polymer composition supply port, and a devolatilized polymer outlet arranged in this order from the driving part side to the tip end side in the axial direction of the screw, and the devolatilizing extruder Part or all of the heat required to volatilize the volatile components is given to the composition in advance, and the composition is supplied to the polymer composition supply port in the state of a gas-liquid mixed flow or a gas-liquid-solid mixed flow, and the volatilized components are A method for devolatilizing a thermoplastic polymer composition, characterized in that the volatile components are passed through a space formed by a cylinder and a screw at a flow rate of 50 m/sec or less and taken out from an outlet of the volatile components.
反応単量体、溶剤及び／または揮発性副生物を含むメタ
クリル酸メチル系重合体組成物である請求項（１）の方
法。(2) The method according to claim (1), wherein the thermoplastic polymer composition is a methyl methacrylate-based polymer composition containing 20 to 70% by weight of unreacted monomer, solvent and/or volatile by-products. .
が５０〜１５００ｍｍＨｇである請求項（１）の方法。(3) The method of claim (1), wherein the pressure at the volatile component outlet of the screw type devolatilizing extruder is 50 to 1500 mmHg.
供給口と揮発成分出口との軸方向距離がスクリュー径を
Ｄとした時、３Ｄ以上である請求項（１）の方法。(4) The method according to claim 1, wherein in the screw type devolatilizing extruder, the axial distance between the polymer composition supply port and the volatile component outlet is 3D or more, where D is the screw diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1185631A JP2782810B2 (en) | 1989-07-17 | 1989-07-17 | Method for devolatilizing extrusion of thermoplastic polymer composition |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1185631A JP2782810B2 (en) | 1989-07-17 | 1989-07-17 | Method for devolatilizing extrusion of thermoplastic polymer composition |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0349925A true JPH0349925A (en) | 1991-03-04 |
| JP2782810B2 JP2782810B2 (en) | 1998-08-06 |
Family
ID=16174157
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1185631A Expired - Fee Related JP2782810B2 (en) | 1989-07-17 | 1989-07-17 | Method for devolatilizing extrusion of thermoplastic polymer composition |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2782810B2 (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5565537A (en) * | 1992-06-17 | 1996-10-15 | Nippon Shokubai Co., Ltd. | Maleimide-based copolymer and process for producing it |
| WO2000044549A1 (en) * | 1999-01-26 | 2000-08-03 | Mitsubishi Rayon Co., Ltd. | Extruding method for volatilization and screw type extrusion machine for volatilization |
| US6100366A (en) * | 1998-09-18 | 2000-08-08 | Nippon Shokubai Co., Ltd. | Cyclic imino ether group containing polymer and production process therefor |
| EP1642638A1 (en) | 2004-10-04 | 2006-04-05 | Sumitomo Chemical Company, Limited | Apparatus for continuous polymerization and method for continuous polymerizing using the same |
| EP1655309A1 (en) | 2004-11-09 | 2006-05-10 | Sumitomo Chemical Company, Limited | Process for stopping continuous polymerization |
| WO2006073168A1 (en) * | 2005-01-07 | 2006-07-13 | Asahi Kasei Chemicals Corporation | Inner part of hard disk drive |
| KR20120005409A (en) | 2010-07-08 | 2012-01-16 | 스미또모 가가꾸 가부시끼가이샤 | Devolatilizing extruder, and devolatilizing extrusion method of polymer composition using the same and method of producing polymer |
| JP2012016886A (en) * | 2010-07-08 | 2012-01-26 | Sumitomo Chemical Co Ltd | Devolatilizing extruder, and devolatilizing extrusion method of polymer composition using the same and method of producing methacryl based polymer |
| EP2450101A1 (en) | 2010-11-08 | 2012-05-09 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2481477A1 (en) | 2011-01-26 | 2012-08-01 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2481476A1 (en) | 2011-01-26 | 2012-08-01 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2500363A1 (en) | 2011-03-17 | 2012-09-19 | Sumitomo Chemical Company Limited | Process for Producing Polymer Composition |
| WO2013073595A1 (en) | 2011-11-18 | 2013-05-23 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| WO2014007271A1 (en) | 2012-07-05 | 2014-01-09 | Sumitomo Chemical Company, Limited | Process for producing methacrylic polymer composition |
| WO2014088082A1 (en) | 2012-12-03 | 2014-06-12 | 住友化学株式会社 | Method for producing methacrylic polymer composition, and molded article |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58147332A (en) * | 1982-02-26 | 1983-09-02 | Sumitomo Chem Co Ltd | Devolatilization extruding method and device thereof |
-
1989
- 1989-07-17 JP JP1185631A patent/JP2782810B2/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58147332A (en) * | 1982-02-26 | 1983-09-02 | Sumitomo Chem Co Ltd | Devolatilization extruding method and device thereof |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5565537A (en) * | 1992-06-17 | 1996-10-15 | Nippon Shokubai Co., Ltd. | Maleimide-based copolymer and process for producing it |
| US6100366A (en) * | 1998-09-18 | 2000-08-08 | Nippon Shokubai Co., Ltd. | Cyclic imino ether group containing polymer and production process therefor |
| WO2000044549A1 (en) * | 1999-01-26 | 2000-08-03 | Mitsubishi Rayon Co., Ltd. | Extruding method for volatilization and screw type extrusion machine for volatilization |
| CN1321793C (en) * | 1999-01-26 | 2007-06-20 | 三菱丽阳株式会社 | Extruding method for volatilization and screw type extrusion machine for volatilization |
| EP1642638A1 (en) | 2004-10-04 | 2006-04-05 | Sumitomo Chemical Company, Limited | Apparatus for continuous polymerization and method for continuous polymerizing using the same |
| EP1655309A1 (en) | 2004-11-09 | 2006-05-10 | Sumitomo Chemical Company, Limited | Process for stopping continuous polymerization |
| WO2006073168A1 (en) * | 2005-01-07 | 2006-07-13 | Asahi Kasei Chemicals Corporation | Inner part of hard disk drive |
| JPWO2006073168A1 (en) * | 2005-01-07 | 2008-08-07 | 旭化成ケミカルズ株式会社 | Hard disk drive internal parts |
| JP4606423B2 (en) * | 2005-01-07 | 2011-01-05 | 旭化成ケミカルズ株式会社 | Hard disk drive internal parts |
| US7932315B2 (en) | 2005-01-07 | 2011-04-26 | Asahi Kasei Chemicals Corporation | Inner part of hard disk drive |
| KR20120005409A (en) | 2010-07-08 | 2012-01-16 | 스미또모 가가꾸 가부시끼가이샤 | Devolatilizing extruder, and devolatilizing extrusion method of polymer composition using the same and method of producing polymer |
| JP2012016886A (en) * | 2010-07-08 | 2012-01-26 | Sumitomo Chemical Co Ltd | Devolatilizing extruder, and devolatilizing extrusion method of polymer composition using the same and method of producing methacryl based polymer |
| EP2450101A1 (en) | 2010-11-08 | 2012-05-09 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2481477A1 (en) | 2011-01-26 | 2012-08-01 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2481476A1 (en) | 2011-01-26 | 2012-08-01 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| EP2500363A1 (en) | 2011-03-17 | 2012-09-19 | Sumitomo Chemical Company Limited | Process for Producing Polymer Composition |
| WO2013073595A1 (en) | 2011-11-18 | 2013-05-23 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| US9266975B2 (en) | 2011-11-18 | 2016-02-23 | Sumitomo Chemical Company, Limited | Continuous polymerization apparatus and process for producing polymer composition |
| WO2014007271A1 (en) | 2012-07-05 | 2014-01-09 | Sumitomo Chemical Company, Limited | Process for producing methacrylic polymer composition |
| WO2014088082A1 (en) | 2012-12-03 | 2014-06-12 | 住友化学株式会社 | Method for producing methacrylic polymer composition, and molded article |
| CN115197354A (en) * | 2022-07-22 | 2022-10-18 | 云南正邦科技有限公司 | Method and system for recycling low-pressure polymerization EVA (ethylene-vinyl acetate) solvent |
| CN115197354B (en) * | 2022-07-22 | 2023-02-10 | 云南正邦科技有限公司 | Method and system for recycling low-pressure polymerization EVA (ethylene-vinyl acetate) solvent |
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