JPH04311703A - Dehydrative extruder - Google Patents
Dehydrative extruderInfo
- Publication number
- JPH04311703A JPH04311703A JP3103637A JP10363791A JPH04311703A JP H04311703 A JPH04311703 A JP H04311703A JP 3103637 A JP3103637 A JP 3103637A JP 10363791 A JP10363791 A JP 10363791A JP H04311703 A JPH04311703 A JP H04311703A
- Authority
- JP
- Japan
- Prior art keywords
- polymer
- extruder
- downstream side
- drain port
- discharged
- 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.)
- Withdrawn
Links
- 238000001914 filtration Methods 0.000 claims abstract description 55
- 239000002994 raw material Substances 0.000 claims abstract description 21
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 14
- 230000018044 dehydration Effects 0.000 claims description 11
- 238000006297 dehydration reaction Methods 0.000 claims description 11
- 238000007906 compression Methods 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 9
- 229920000642 polymer Polymers 0.000 abstract description 44
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 18
- 239000007788 liquid Substances 0.000 abstract description 13
- 238000003825 pressing Methods 0.000 abstract description 8
- 238000001035 drying Methods 0.000 abstract description 7
- 239000002904 solvent Substances 0.000 abstract description 6
- 239000011347 resin Substances 0.000 abstract description 2
- 229920005989 resin Polymers 0.000 abstract description 2
- 229920003051 synthetic elastomer Polymers 0.000 abstract description 2
- 239000005061 synthetic rubber Substances 0.000 abstract description 2
- 229920001169 thermoplastic Polymers 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 13
- 239000002245 particle Substances 0.000 description 10
- 238000002474 experimental method Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 238000001125 extrusion Methods 0.000 description 6
- 238000004898 kneading Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005469 granulation Methods 0.000 description 4
- 230000003179 granulation Effects 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000007720 emulsion polymerization reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010559 graft polymerization reaction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000004816 latex Substances 0.000 description 1
- 229920000126 latex Polymers 0.000 description 1
- 229920002857 polybutadiene Polymers 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material 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
- B29C48/761—Venting, drying means; Degassing means the vented material being in liquid form
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
Abstract
Description
【０００１】0001
【産業上の利用分野】本発明は、ＡＢＳ樹脂、合成ゴム
、ＭＭＡ樹脂等の重合された後、多量に水または溶剤を
含有する熱可塑性重合体（以下単に重合体という）を脱
水、乾燥、押出造粒する脱水押出機に係わるもので、排
液口の濾過装置から排出される水または溶剤に同伴され
て排出される重合体（以下単にリークポリマーという）
を最小限にする装置に関する。[Industrial Application Field] The present invention deals with dehydrating, drying, and drying thermoplastic polymers (hereinafter simply referred to as polymers) containing a large amount of water or solvent after being polymerized, such as ABS resin, synthetic rubber, and MMA resin. This is related to a dehydration extruder that performs extrusion granulation, and the polymer is discharged along with the water or solvent discharged from the filtration device at the drainage port (hereinafter simply referred to as leak polymer).
This invention relates to a device that minimizes
【０００２】0002
【従来の技術】従来、水または溶剤を多量に含有した重
合体から乾燥した重合体を回収する方法としては、重合
体に、必要に応じ凝固処理を施し、濾過機や遠心分離機
等により脱水し、熱風乾燥機等で乾燥した後、押出機で
押出造粒する方法が多く用いられている。しかし、この
方法はエネルギー消費が大きいことから、濾過機や遠心
分離機等で脱水した重合体、あるいは脱水前のスラリー
状の重合体を原料に、圧搾、乾燥、押出造粒を１基の装
置で行う方法（特開昭５４−１３９６６８号公報、特公
昭５９−３７０２１号公報、特公昭６１−５３３６２号
公報、特開平２−１８９３０４号公報等）やラテックス
状の重合体と凝固剤を原料に、凝固、圧搾、乾燥、押出
造粒を１基の装置で行う方法（特公昭５０−１７２２７
号公報、特公昭６０−１０８８４号公報等）などが開発
されてきた。[Prior Art] Conventionally, as a method for recovering dried polymers from polymers containing a large amount of water or solvent, the polymers are subjected to coagulation treatment as necessary, and then dehydrated using a filter, centrifuge, etc. However, after drying using a hot air dryer or the like, extrusion granulation using an extruder is often used. However, since this method consumes a large amount of energy, it uses a polymer dehydrated using a filter or centrifugal separator, or a slurry-like polymer before dehydration as raw material, and processes compression, drying, and extrusion granulation in one machine. (JP-A-54-139668, JP-A-59-37021, JP-A-61-53362, JP-A-2-189304, etc.) or using a latex-like polymer and a coagulant as raw materials. , a method in which coagulation, compression, drying, and extrusion granulation are performed in one device (Japanese Patent Publication No. 50-17227)
No. 60-10884, etc.) have been developed.
【０００３】0003
【発明が解決しようとする課題】しかしながら、脱水押
出機には、排液口に設けられた濾過装置から排液と共に
重合体も排出され重合体の回収率が低下するという欠点
がある。これは、重合体が、粒度分布の比較的狭いサス
ペンション重合による粒子であっても、乳化重合ラテッ
クスの凝固処理を改善（特開昭６０−１６３９３３号公
報、特開昭６２−１７０３号公報、特開昭６２−３０１
０６号公報等）して大きくした粒子であっても、押出機
中で重合体が破砕されるので、避けることができない。
また、排液口の目開きを小さくしてリークポリマーの削
減を図ると、濾過面積が多く必要となる。よって通常は
、リークポリマー量と脱水面積のバランスをとって、排
液口の濾過装置の目開きを設定している。However, the dewatering extruder has the disadvantage that the polymer is also discharged together with the waste liquid from a filtration device provided at the drain port, resulting in a decrease in the recovery rate of the polymer. This improves the coagulation process of emulsion polymerization latex even if the polymer is suspension polymerized particles with a relatively narrow particle size distribution (Japanese Patent Laid-Open Nos. 60-163933, 1982-1703, Kaisho 62-301
Even if the particles are made larger using a method such as that disclosed in Japanese Patent No. 06, the polymer is crushed in the extruder, which is unavoidable. Furthermore, if the opening of the drainage port is made smaller to reduce the amount of leaked polymer, a large filtration area will be required. Therefore, the opening of the filtration device at the drain port is usually set to balance the amount of leaked polymer and the dewatering area.
【０００４】ところが、複数の銘柄を生産しようとする
場合、各銘柄とも均一の粒径にするには困難があり、ま
た脱水押出機内部での破砕状況も異なるのが通常である
ので、各銘柄ごとに排液口の濾過装置の目開きの最適値
が異なる。更に、同一銘柄においても、定常時の運転の
乱れ、スタートアップ、シャットダウン、銘柄切り替え
のときには、粒径を一定に保つのは困難である。従って
、従来は粒子の変化に対応して、濾過装置を目開きの適
正なものに交換する、濾過装置の目開きを大き目に設定
する、濾過装置の目開きを小さ目に設定して濾過面積を
大きくとるなどの対応が必要である。However, when trying to produce multiple brands, it is difficult to make each brand have a uniform particle size, and the crushing conditions inside the dehydration extruder usually differ, so each brand The optimal value for the opening of the drainage port filtration device differs depending on the type. Furthermore, even for the same brand, it is difficult to keep the particle size constant during normal operation, startup, shutdown, and brand switching. Therefore, in the past, in response to changes in particles, the filtration area could be increased by replacing the filtration device with one with an appropriate opening, setting the filtration device's opening to a larger one, or setting the filtration device's opening to a smaller one. It is necessary to take measures such as making it larger.
【０００５】しかしながら、濾過装置を適正なものに交
換する対応では、交換に人手がかかり、装置も交換の間
、停止する必要がありロスが大きいことや、予期しない
運転の乱れに対しては対応できないという欠点を有する
。濾過装置の目開きを大き目に設定すると、リークポリ
マーが増加するという欠点を有する。濾過面積を大きく
とるには、脱水押出機のスクリューの径を大きくする、
バレル、スクリューを長くして排水溝排液口を増やすな
どの対策が必要であり、設備投資額と消費動力が増すな
どの欠点がある。[0005] However, replacing the filtration device with a proper one requires manpower, the device must be stopped during replacement, resulting in large losses, and it is difficult to deal with unexpected operational disturbances. It has the disadvantage that it cannot. Setting the opening of the filtration device to be large has the drawback of increasing leakage polymer. To increase the filtration area, increase the diameter of the dehydration extruder screw.
It requires measures such as lengthening the barrel and screw and increasing the number of drainage holes in the drain, which has disadvantages such as increased capital investment and power consumption.
【０００６】本発明の目的は、銘柄の違いや定常時の運
転の乱れ、スタートアップ、シャットダウン、銘柄切り
替えのときに発生する異なった粒径の原料に対して、リ
ークポリマーが少なく、濾過装置の交換を必要としない
安価な脱水押出機を与えることである。[0006] The purpose of the present invention is to minimize the amount of leaked polymer and to make it easier to replace filtration equipment for raw materials with different particle sizes that occur during different brands, disturbances in steady-state operation, startup, shutdown, and brand switching. The objective is to provide an inexpensive dewatering extruder that does not require
【０００７】[0007]
【課題を解決するための手段】本発明は、原料供給口よ
り下流側に排液口、さらに下流側に圧搾部を設けた脱水
押出機において、排液口に、上流側の目開きを大きく下
流側の目開きを小さくした濾過装置を配したことを特徴
とする脱水押出機である。[Means for Solving the Problems] The present invention provides a dewatering extruder which is provided with a drain port on the downstream side of the raw material supply port and a compression section further downstream. This dewatering extruder is characterized by being equipped with a filtration device with small openings on the downstream side.
【０００８】濾過装置の上流側の目開きを大きく、下流
側の目開きを小さくした装置として、例えば■１つの圧
搾部に対し、それに対応する排液口を原料流れ方向に直
列に２箇所以上設け、上流側の排液口ほど目開きの大き
な濾過装置を配した脱水押出機、■濾過装置を下流側が
太くなるウェッジワイヤーを用いて構成し、上流側の目
開きを大きく、下流側の目開きを小さくした脱水押出機
や■両者の組み合わせなどがある。濾過装置としては、
例えば、メッシュスクリーン、パンチングプレート、ゲ
ージバー、ウェッジワイヤースクリーン等を用いること
ができるが、強度、目開きサイズの精度、目詰まり防止
等の面で優れるウェッジワイヤースクリーンが好適であ
る。[0008] As a device in which the opening on the upstream side of the filtration device is large and the opening on the downstream side is small, for example: (1) For one pressing section, two or more corresponding drain ports are arranged in series in the raw material flow direction. The dewatering extruder is equipped with a filtration device with larger openings on the upstream side, and the filtration device is constructed using a wedge wire that becomes thicker on the downstream side, with larger openings on the upstream side and larger openings on the downstream side. There are dehydration extruders with small openings and combinations of both. As a filtration device,
For example, a mesh screen, a punching plate, a gauge bar, a wedge wire screen, etc. can be used, but a wedge wire screen is preferable because it is excellent in terms of strength, accuracy of opening size, prevention of clogging, etc.
【０００９】圧搾部とは、重合体を圧縮し、剪断を与え
る部分であり、単軸押出機では、例えばスクリューの谷
径を徐々に大きくしたり、リングを用いて構成する。２
軸押出機では、例えば順ネジスクリューのほか、逆ネジ
スクリュー、リング、ニーディングディスク、ローター
等で構成することができる。圧搾部は複数箇所設けるこ
とが多いが、それに対応する排液口全てに本発明を適用
しても構わないが、排出される液量が少ない排液口に適
用しても効果は少ない。また、圧搾部が複数箇所ある場
合、排液口に上流側の目開きを大きく、下流側の目開き
を小さくした濾過装置を配するというのは、同一圧搾部
に対応する排液口の範囲内のことであり、排液口に対応
する圧搾部が異なれば、本発明の効果は、及ばない。[0009] The compression section is a section that compresses the polymer and applies shear, and in a single-screw extruder, it is constructed, for example, by gradually increasing the root diameter of a screw or by using a ring. 2
The axial extruder can be configured with, for example, not only a forward-threaded screw but also a reverse-threaded screw, a ring, a kneading disk, a rotor, and the like. Although a plurality of squeezing portions are often provided, the present invention may be applied to all of the corresponding drain ports, but the effect will be small even if the present invention is applied to a drain port that discharges a small amount of liquid. In addition, when there are multiple squeezing sections, installing a filtration device with larger openings on the upstream side and smaller openings on the downstream side means that the range of drain ports corresponding to the same squeezing section is However, if the squeezing portion corresponding to the drain port is different, the effects of the present invention will not be as great.
【００１０】押出機は、単軸，２軸のいずれでもよいが
、とくに、２軸押出機は、単軸押出機に比べセルフクリ
ーニング性、混練性、運転の安定性などにおいて優れて
おり、また、そのうちでも同方向回転２軸押出機は、異
方向回転２軸押出機に比べ圧搾部で絞った液が圧搾部よ
り上流側にある排液口まで流れ易いので、同方向回転２
軸押出機が好適である。[0010] The extruder may be either a single-screw or twin-screw extruder, but a twin-screw extruder is particularly superior to a single-screw extruder in terms of self-cleaning performance, kneading performance, operational stability, etc. Among them, the co-rotating twin-screw extruder makes it easier for the liquid squeezed in the squeezing part to flow to the drain port located upstream from the squeezing part, compared to the opposite-rotating twin-screw extruder.
A screw extruder is preferred.
【００１１】次に、図１および図２により、本発明を詳
細に説明する。図１は、本発明の一例である２軸脱水押
出機のバレルおよびスクリューの構成図であり、図２は
、圧搾部８、９付近の拡大図および運転中の圧力を表し
た図である。供給口１より供給された重合体は圧搾部８
で圧搾される。絞り出された水あるいは溶剤（以下水等
という）は、図２の圧力勾配に沿って逆流し排液口２ｂ
から排出される。水等は、排液口２ｂの下流側から排出
され、量が増加するに従って、順に上流側からも排出さ
れるようになり、さらに量が増加すると排液口２ａの下
流側へと排液範囲が広がっていく。Next, the present invention will be explained in detail with reference to FIGS. 1 and 2. FIG. 1 is a configuration diagram of a barrel and screw of a twin-screw dewatering extruder which is an example of the present invention, and FIG. 2 is an enlarged view of the vicinity of the pressing sections 8 and 9 and a diagram showing the pressure during operation. The polymer supplied from the supply port 1 is transferred to the compression section 8
is squeezed with The squeezed out water or solvent (hereinafter referred to as water, etc.) flows back along the pressure gradient shown in Fig. 2 to the drain port 2b.
is discharged from. Water, etc. is discharged from the downstream side of the drain port 2b, and as the amount increases, it is sequentially discharged from the upstream side, and when the amount increases further, the drain range is extended to the downstream side of the drain port 2a. is spreading.
【００１２】圧搾部８を通過した重合体は、圧搾部９で
さらに圧搾されて含液率を下げる。圧搾部９で絞り出さ
れた水等は、排液口３から、液体のまま、あるいは蒸気
となって排出される。圧搾部９を通過した重合体はベン
ト部４、５において図示されていない真空ポンプによっ
て減圧に吸引され、さらに脱揮乾燥されて、先端ノズル
より乾燥重合体として押し出される。The polymer that has passed through the compression section 8 is further compressed in the compression section 9 to lower the liquid content. The water squeezed out by the squeezing part 9 is discharged from the drain port 3 either as a liquid or in the form of steam. The polymer that has passed through the pressing section 9 is sucked to a reduced pressure by a vacuum pump (not shown) in the vent sections 4 and 5, is further devolatilized and dried, and is extruded from the tip nozzle as a dry polymer.
【００１３】ここで排液口２ｂ、２ａからは、水等に伴
われて重合体が１〜数％排出される。従来技術では、最
も濾過面積を必要とする銘柄の重合体（Ａ）を所定のレ
ートで処理する場合、リークポリマーを少なくするには
、排液口の濾過装置の目開きを小さくするが、それに伴
って濾過面積が増加し、ついには排液口２ｂおよび排液
口２ａ全面を使っても排出しきれなくなる。そうすると
、供給口１付近の輸送能力が落ち、重合体を所定のレー
トで供給できなくなる、あるいは、脱水不足の重合体が
ベント部４に供給され脱揮量が増加するので、重合体が
蒸気に同伴されて飛散し運転不能になる。従って、排液
部の面積とリークポリマーの量のバランスをとり、運転
の乱れを考慮して、かなり濾過面積に余裕をもって、通
常５０％程度の濾過面積を使用する程度に調整された目
開きの濾過装置（Ｘ）にする。Here, from the drain ports 2b and 2a, 1 to several percent of the polymer is discharged along with water and the like. In the conventional technology, when processing the brand of polymer (A) that requires the most filtration area at a predetermined rate, the opening of the filtration device at the drain port is made smaller in order to reduce the amount of leaked polymer. As a result, the filtration area increases, and eventually the liquid cannot be completely drained even if the entire surface of the liquid drain port 2b and the liquid drain port 2a are used. If this happens, the transport capacity near the supply port 1 will decrease, making it impossible to supply the polymer at a predetermined rate, or insufficiently dehydrated polymer will be supplied to the vent section 4 and the amount of devolatilization will increase, causing the polymer to turn into steam. They are carried away and scattered, making it impossible to drive. Therefore, by balancing the area of the drainage part and the amount of leaked polymer, and taking into account operational disturbances, the opening of the mesh is adjusted to the extent that normally about 50% of the filtration area is used, with a considerable margin for the filtration area. Turn on the filtration device (X).
【００１４】一方、同一押出機で濾過面積の余りいらな
い銘柄の重合体（Ｂ）を処理する場合、リークポリマー
の量を少なくするため、より目開きの小さい濾過装置（
Ｙ）に取り替えるか、または、手段を講じればリークポ
リマーを削減できるにもかかわらずリークポリマーの多
いまま運転を継続しなければならない。On the other hand, when using the same extruder to process a brand of polymer (B) that does not require much filtration area, a filtration device with smaller openings (
Although it is possible to reduce the amount of leaked polymer by replacing it with Y) or by taking other measures, operation must be continued with a large amount of leaked polymer.
【００１５】本発明の一例は、目開きの大きい濾過装置
（Ｘ）を上流側排液口２ａに配し、目開きの小さい濾過
装置（Ｙ）を下流側排液口２ｂに配した２軸脱水押出機
である。排液口は下流側から順に使用されるので、銘柄
（Ｂ）を処理するときには、排液口２ｂが使用され、リ
ークポリマーが少ない運転がなされる。銘柄（Ａ）を処
理するときにも、同一濾過装置のまま運転されるが、濾
過装置（Ｙ）の不足分は、目開きの大きい濾過装置（Ｘ
）で補われるため濾過面積が不足することはない。
むしろ、排液のかなりの部分が目開きの小さい濾過装置
（Ｙ）でなされるため、リークポリマー量は、従来装置
で処理する場合より減少する。An example of the present invention is a two-shaft system in which a filtration device (X) with a large opening is arranged at the upstream drain port 2a, and a filtration device (Y) with a small opening is arranged at the downstream drain port 2b. This is a dehydration extruder. Since the drain ports are used in order from the downstream side, when processing brand (B), the drain port 2b is used, and operation with less leaked polymer is performed. When processing brand (A), the same filtration device is operated, but the shortage of filtration device (Y) is replaced by a filtration device with a larger opening (X
), so there is no shortage of filtration area. On the contrary, since a considerable portion of the liquid is drained through the filtration device (Y) with small openings, the amount of leaked polymer is reduced compared to the case of processing with the conventional device.
【００１６】この例では排液口が２ａ、２ｂの２箇所に
ある場合について述べたが、圧搾部８に対応する排液口
が１箇所しかない場合は、１つの排液口に、上流側の目
開きを大きく、下流側の目開きを小さくした濾過装置、
例えば、下流側が太くなるウェッジワイヤーを用いて構
成し、上流側の目開きを大きく、下流側の目開きを小さ
くした濾過装置を用いれば同様の効果があるのは言うま
でもない。[0016] In this example, the case where there are two drainage ports 2a and 2b has been described, but if there is only one drainage port corresponding to the squeezing part 8, one drainage port is provided at the upstream side. A filtration device with a large opening on the downstream side and a small opening on the downstream side,
For example, it goes without saying that a similar effect can be obtained by using a filtration device that is constructed using a wedge wire that is thicker on the downstream side, with larger openings on the upstream side and smaller openings on the downstream side.
【００１７】ところで、排液口の部分の圧力は図２の圧
搾部より上流側であり小さいので、押出機がスクリュー
径２００ｍｍ程度の大型になると、重力の影響が出て、
濾過装置の下部が余計に排液に使用されるようになる。
その場合、濾過装置の目開きを下部ほど小さくしておく
のも有効である。By the way, the pressure at the drain port is on the upstream side of the squeezing section in FIG. 2 and is small, so when the extruder becomes large with a screw diameter of about 200 mm, the influence of gravity comes into play.
The lower part of the filtration device is now used for drainage. In that case, it is also effective to make the opening of the filtration device smaller toward the bottom.
【００１８】[0018]
【実施例】さらに、実施例で具体的に述べる。原料とし
てＡＢＳ系樹脂を用いて、比較を行った。原料ＡＢＳ系
樹脂は、ポリブタジエンゴムにアクリロニトリル、スチ
レン、必要に応じてさらにαメチルスチレンを乳化グラ
フト重合したものを、凝固処理、肥大化処理した後、遠
心濾過機で脱水したものを用いた。銘柄（Ａ）に相当す
るもの（以後銘柄Ａという）として、αメチルスチレン
も共重合したものを、銘柄（Ｂ）に相当するもの（以後
銘柄Ｂという）として、αメチルスチレンを含有しない
ものを用いた。銘柄Ａの５０％粒径は８００ミクロンで
あり銘柄Ｂの５０％粒径は４５０ミクロンであったが、
銘柄Ａは破砕されやすく、脱水面積が多く必要な銘柄と
なった。含水率はいずれも８０％であった。ここで、含
水率とは水分量／（含水ＡＢＳ−水分量）で定義される
ドライベースのものをいう。[Example] Further, the following will be described in detail in an example. A comparison was made using ABS resin as the raw material. The raw material ABS resin used was one obtained by emulsion graft polymerization of polybutadiene rubber with acrylonitrile, styrene, and if necessary α-methylstyrene, which was coagulated and enlarged, and then dehydrated with a centrifugal filter. An equivalent to brand (A) (hereinafter referred to as brand A) is one that also copolymerizes α-methylstyrene, and one equivalent to brand (B) (hereinafter referred to as brand B) is one that does not contain α-methylstyrene. Using. The 50% particle size of brand A was 800 microns and the 50% particle size of brand B was 450 microns.
Brand A was easily crushed and required a large area for dewatering. The moisture content was 80% in all cases. Here, the moisture content refers to a dry base defined as moisture content/(hydrated ABS-moisture content).
【００１９】脱水押出機は、互いに噛み合わせて同方向
に回転するスクリューを有する２軸押出機で、スクリュ
ー径７０ｍｍのもの、バレルおよびスクリュー構成を図
１の様に組んだものを用い、濾過装置はウェッジワイヤ
ースクリーンの目開き０．３ｍｍおよび０．２ｍｍのも
のをそれぞれ（Ｘ）および（Ｙ）に相当するものとして
用いた。以下各々（Ｘ）、（Ｙ）という。また上流側目
開き０．３ｍｍ下流側目開き０．２ｍｍの特殊なウェッ
ジワイヤースクリーン（以下（Ｚ）という）も用いた。
圧搾部８、９は図２に示す如く、順ネジスクリュー２１
、順送りニーディングディスク２２、逆送りニーディン
グディスク２２、逆ネジスクリュー２３の組合せを用い
た。The dehydration extruder is a twin-screw extruder having screws that mesh with each other and rotate in the same direction, with a screw diameter of 70 mm, and a barrel and screw configuration assembled as shown in Figure 1. Wedge wire screens with openings of 0.3 mm and 0.2 mm were used as equivalents to (X) and (Y), respectively. Hereinafter, they will be referred to as (X) and (Y), respectively. A special wedge wire screen (hereinafter referred to as (Z)) with an upstream opening of 0.3 mm and a downstream opening of 0.2 mm was also used. As shown in FIG.
, a combination of a forward kneading disk 22, a reverse kneading disk 22, and a reverse thread screw 23 was used.
【００２０】押出条件は、実施例、比較例とも、また銘
柄（Ａ）、（Ｂ）とも同一で、処理レートは、固形分と
して２００Ｋｇ／Ｈ、スクリュー回転数は２５０回転／
分とした。バレル温度の設定は、供給口１、排液口２ａ
、２ｂ、３は、過熱冷却せず、他は２００℃にコントロ
ールした。The extrusion conditions were the same for both Examples and Comparative Examples as well as brands (A) and (B); the processing rate was 200 kg/H as a solid content, and the screw rotation speed was 250 rpm.
It was a minute. Barrel temperature settings are at supply port 1 and drain port 2a.
, 2b, and 3 were not superheated and cooled, and the others were controlled at 200°C.
【００２１】結果を表１にまとめた。表中、濾過装置使
用率とは、スクリーンのうち水が排出されている部分の
ことであり、目視で確認を行った。[0021] The results are summarized in Table 1. In the table, the filtration device usage rate refers to the portion of the screen from which water is discharged, and was visually confirmed.
【００２２】［実施例１］排液口２ａに（Ｘ）を、排液
口２ｂに（Ｙ）を配し、原料は銘柄（Ａ）を用いて実験
を行った。運転は安定に行われ、排液口２ａは濾過面積
の３０％からＡＢＳ系樹脂を含んだ水が排出され、排液
口２ｂは濾過面積の全面からＡＢＳ系樹脂を含んだ水が
排出された。排水は排液口２ａと２ｂあわせて、１４０
Ｋｇ／Ｈ、内ＡＢＳ系樹脂が７Ｋｇ／Ｈで排出された。
排液口３からは液およびＡＢＳ系樹脂はほとんど排出さ
れず、蒸気が排出された。先端ノズル６からは溶融した
ＡＢＳ系樹脂が安定して排出されガスの噴出はなかった
。[Example 1] An experiment was conducted using (X) at the drain port 2a and (Y) at the drain port 2b, and using brand (A) as the raw material. The operation was stable, and water containing ABS resin was discharged from 30% of the filtration area from the drain port 2a, and water containing ABS resin was discharged from the entire filtration area from the drain port 2b. . The drainage capacity is 140 mm including drain ports 2a and 2b.
kg/h, of which ABS resin was discharged at 7 kg/h. Almost no liquid or ABS resin was discharged from the liquid drain port 3, but only steam was discharged. The molten ABS resin was stably discharged from the tip nozzle 6, and no gas was ejected.
【００２３】［実施例２］原料を銘柄（Ｂ）としたほか
は実施例１と同じ条件で実験を行った。運転は安定に行
われ、排液口２ａは使われず、排液口２ｂは濾過面積の
７０％からＡＢＳ系樹脂を含んだ水が排出された。排水
は、排液口２ｂから１４５Ｋｇ／Ｈ、内ＡＢＳ系樹脂が
３Ｋｇ／Ｈで排出された。その他は実施例１と同様の結
果であった。[Example 2] An experiment was conducted under the same conditions as in Example 1 except that the raw material was used as brand (B). The operation was carried out stably, the drain port 2a was not used, and water containing ABS resin was discharged from 70% of the filtration area of the drain port 2b. The waste water was discharged from the drain port 2b at a rate of 145 kg/h, and the ABS resin was discharged at a rate of 3 kg/h. Other results were the same as in Example 1.
【００２４】［実施例３］排液口２ａに（Ｘ）を、排液
口２ｂに（Ｚ）を配し、原料は銘柄（Ａ）を用いて実験
を行った。運転は安定に行われ、排液口２ａは使われず
、排液口２ｂは濾過面積の９５％からＡＢＳ系樹脂を含
んだ水が排出された。排水は排液口２ｂから、１４５Ｋ
ｇ／Ｈ、内ＡＢＳ系樹脂が８Ｋｇ／Ｈで排出された。
その他は実施例１と同様の結果であった。[Example 3] An experiment was conducted using (X) at the drain port 2a and (Z) at the drain port 2b, and using brand (A) as the raw material. The operation was stable, the drain port 2a was not used, and water containing ABS resin was discharged from 95% of the filtration area of the drain port 2b. Drainage is from drain port 2b, 145K
g/h, of which ABS resin was discharged at 8 kg/h. Other results were the same as in Example 1.
【００２５】［実施例４］原料を銘柄（Ｂ）としたほか
は実施例３と同じ条件で実験を行った。運転は安定に行
われ、排液口２ａは使われず、排液口２ｂは濾過面積の
５０％からＡＢＳ系樹脂を含んだ水が排出された。排水
は、排液口２ｂから１４５Ｋｇ／Ｈ、内ＡＢＳ系樹脂が
４Ｋｇ／Ｈで排出された。その他は実施例１と同様の結
果であった。[Example 4] An experiment was conducted under the same conditions as in Example 3 except that the raw material was used as brand (B). The operation was stable, the drain port 2a was not used, and the water containing ABS resin was discharged from 50% of the filtration area of the drain port 2b. The waste water was discharged from the drain port 2b at a rate of 145 Kg/H, and the ABS resin was discharged at a rate of 4 Kg/H. Other results were the same as in Example 1.
【００２６】［比較例１］排液口２ａ、排液口２ｂとも
に（Ｘ）を配し、原料は銘柄（Ａ）を用いて実験を行っ
た。運転は安定に行われ、排液口２ａは使われず、排液
口２ｂは濾過面積の７０％からＡＢＳ系樹脂を含んだ水
が排出された。排水は排液口２ｂから１４５Ｋｇ／Ｈ、
内ＡＢＳ系樹脂が１０Ｋｇ／Ｈで排出された。その他は
実施例１と同様の結果であった。[Comparative Example 1] An experiment was conducted using (X) in both the drain port 2a and the drain port 2b, and brand (A) as the raw material. The operation was carried out stably, the drain port 2a was not used, and water containing ABS resin was discharged from 70% of the filtration area of the drain port 2b. Drainage is 145Kg/H from drain port 2b,
ABS resin was discharged at a rate of 10 kg/h. Other results were the same as in Example 1.
【００２７】［比較例２］原料を銘柄（Ｂ）としたほか
は比較例１と同じ条件で実験を行った。運転は安定に行
われ、排液口２ａは使われず、排液口２ｂは濾過面積の
２５％からＡＢＳ系樹脂を含んだ水が排出された。排水
は、排液口２ｂから１４０Ｋｇ／Ｈ、内ＡＢＳ系樹脂が
６Ｋｇ／Ｈで排出された。その他は実施例１と同様の結
果であった。[Comparative Example 2] An experiment was conducted under the same conditions as Comparative Example 1 except that the raw material was brand (B). The operation was stable, the drain port 2a was not used, and water containing ABS resin was discharged from the drain port 2b from 25% of the filtration area. The waste water was discharged from the drain port 2b at a rate of 140 kg/h, and the ABS resin was discharged at a rate of 6 kg/h. Other results were the same as in Example 1.
【００２８】［比較例３］排液口２ａ、排液口２ｂとも
に（Ｙ）を配し、原料は銘柄（Ａ）を用いて実験を行っ
た。排液口２ａ、２ｂとも全面が使用されたが、面積不
足で供給口１で原料が食い込まなくなった。[Comparative Example 3] An experiment was conducted using (Y) in both the drain port 2a and the drain port 2b, and brand (A) as the raw material. Although the entire surface of both drain ports 2a and 2b was used, the feed port 1 was unable to feed the raw material due to insufficient area.
【００２９】［比較例４］原料を銘柄（Ｂ）としたほか
は比較例３と同じ条件で実験を行った。運転は安定に行
われ、排液口２ａは使われず、排液口２ｂは濾過面積の
７０％からＡＢＳ系樹脂を含んだ水が排出された。排水
は、排液口２ｂから１４０Ｋｇ／Ｈ、内ＡＢＳ系樹脂が
３Ｋｇ／Ｈで排出された。その他は実施例１と同様の結
果であった。[Comparative Example 4] An experiment was conducted under the same conditions as Comparative Example 3 except that the raw material was brand (B). The operation was carried out stably, the drain port 2a was not used, and water containing ABS resin was discharged from 70% of the filtration area of the drain port 2b. The waste water was discharged from the drain port 2b at a rate of 140 kg/h, and the ABS resin was discharged at a rate of 3 kg/h. Other results were the same as in Example 1.
【００３０】[0030]
【表１】[Table 1]
【００３１】[0031]
【発明の効果】濾過装置の目開きを一定にした従来の装
置では、目開きを小さ目に設定すると比較例３のように
、濾過面積を多く必要とする銘柄（Ａ）では、運転不能
になる。また、目開きを大き目に設定すると、比較例１
は実施例１、実施例３より、比較例２は実施例２、実施
例４よりリークポリマーが多くなる。これに対し、本発
明の装置では濾過装置を銘柄ごとに取り替えずに運転す
るにもかかわらず、従来の装置で銘柄ごとに適した目開
きに濾過装置を取り替えて運転した時、つまり、比較例
１と比較例４よりも、リークポリマーが少なく（実施例
１、実施例２）または、総合的に対等（実施例３、実施
例４）にできる。つまり本発明の装置を用いれば、濾過
装置の交換をしなくても、銘柄の違いや定常時の運転の
乱れ、スタートアップ、シャットダウン、銘柄切り替え
のときに発生する異なった粒径の原料に対して、リーク
ポリマーが少い脱水押出が可能となる。[Effect of the invention] In a conventional device in which the opening of the filtration device is fixed, if the opening is set to a small value, the brand (A) that requires a large filtration area, as in Comparative Example 3, becomes inoperable. . Also, if the eye opening is set large, Comparative Example 1
The amount of leaked polymer is larger in Comparative Example 2 than in Examples 1 and 3. On the other hand, although the device of the present invention is operated without replacing the filtration device for each brand, when the conventional device is operated with the filtration device replaced with the appropriate mesh size for each brand, in other words, in the comparative example Compared to Comparative Example 1 and Comparative Example 4, the amount of leaked polymer was smaller (Example 1, Example 2), or the leakage polymer could be made to be on the same level overall (Example 3, Example 4). In other words, if the device of the present invention is used, it is possible to handle raw materials with different particle sizes that occur during startup, shutdown, and brand switching, without having to replace the filtration device. , it becomes possible to perform dehydration extrusion with less leaked polymer.
【図１】本発明の一例である２軸脱水押出機のバレルお
よびスクリューの構成図。FIG. 1 is a configuration diagram of a barrel and screw of a twin-screw dewatering extruder that is an example of the present invention.
【図２】圧搾部（図１、８または９）付近の拡大図およ
び圧力分布を示す図。FIG. 2 is an enlarged view of the vicinity of the pressing section (FIG. 1, 8 or 9) and a diagram showing the pressure distribution.
１ 供給口 ２ａ，２ｂ，３ 排液口 ４，５ ベント ６ ノズル ７ 順ネジスクリュー ８，９ 圧搾部 １０ シール部 ２１ 順ネジスクリュー ２２ 順送りニーディングディスク ２３ 逆送りニーディングディスク ２４ 逆ネジスクリュー ２５ 順ネジスクリュー 1 Supply port 2a, 2b, 3 Drain port 4,5 Vent 6 Nozzle 7 Normal thread screw 8,9 Compression part 10 Seal part 21 Normal thread screw 22 Progressive kneading disc 23 Reverse feed kneading disc 24 Reverse thread screw 25 Normal thread screw
Claims (2)
に下流側に圧搾部を設けた脱水押出機において、該排液
口に、上流側の目開きを大きく下流側の目開きを小さく
した濾過装置を配したことを特徴とする脱水押出機。Claim 1: In a dewatering extruder that is provided with a drain port downstream of a raw material supply port and a compression section further downstream, the drain port is provided with a mesh opening on the upstream side and a small mesh opening on the downstream side. A dehydration extruder characterized by being equipped with a filtration device.
方向に回転するスクリューを有する２軸押出機であるこ
とを特徴とする請求項１記載の脱水押出機。2. The dehydration extruder according to claim 1, wherein the dehydration extruder is a twin-screw extruder having screws that mesh with each other and rotate in the same direction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3103637A JPH04311703A (en) | 1991-04-10 | 1991-04-10 | Dehydrative extruder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3103637A JPH04311703A (en) | 1991-04-10 | 1991-04-10 | Dehydrative extruder |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04311703A true JPH04311703A (en) | 1992-11-04 |
Family
ID=14359285
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3103637A Withdrawn JPH04311703A (en) | 1991-04-10 | 1991-04-10 | Dehydrative extruder |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04311703A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0683028A1 (en) * | 1994-05-19 | 1995-11-22 | Röhm GmbH | Method of dehydrating a water containing resin melt in a twin screw extruder |
| KR20180014821A (en) * | 2015-06-05 | 2018-02-09 | 사빅 글로벌 테크놀러지스 비.브이. | The dehydration method of the polymer and the polymer produced therefrom |
-
1991
- 1991-04-10 JP JP3103637A patent/JPH04311703A/en not_active Withdrawn
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0683028A1 (en) * | 1994-05-19 | 1995-11-22 | Röhm GmbH | Method of dehydrating a water containing resin melt in a twin screw extruder |
| KR20180014821A (en) * | 2015-06-05 | 2018-02-09 | 사빅 글로벌 테크놀러지스 비.브이. | The dehydration method of the polymer and the polymer produced therefrom |
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| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Application deemed to be withdrawn because no request for examination was validly filed |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 19980711 |