JPS6149094B2 - - Google Patents
Info
- Publication number
- JPS6149094B2 JPS6149094B2 JP56191906A JP19190681A JPS6149094B2 JP S6149094 B2 JPS6149094 B2 JP S6149094B2 JP 56191906 A JP56191906 A JP 56191906A JP 19190681 A JP19190681 A JP 19190681A JP S6149094 B2 JPS6149094 B2 JP S6149094B2
- Authority
- JP
- Japan
- Prior art keywords
- temperature
- resin
- cylinder
- extruder
- zone
- 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
Links
- 239000011347 resin Substances 0.000 claims description 72
- 229920005989 resin Polymers 0.000 claims description 72
- 238000000034 method Methods 0.000 claims description 23
- 238000010137 moulding (plastic) Methods 0.000 claims description 8
- 238000009529 body temperature measurement Methods 0.000 description 8
- 238000001125 extrusion Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 235000012438 extruded product Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000000465 moulding Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000003431 cross linking reagent Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000001746 injection moulding Methods 0.000 description 1
- 229920001684 low density polyethylene Polymers 0.000 description 1
- 239000004702 low-density polyethylene Substances 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 229920002545 silicone oil Polymers 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
- B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
- B29C48/80—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling at the plasticising zone, e.g. by heating cylinders
- B29C48/83—Heating or cooling the cylinders
- B29C48/834—Cooling
-
- 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
- B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
- B29C48/80—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling at the plasticising zone, e.g. by heating cylinders
- B29C48/83—Heating or cooling the cylinders
-
- 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
- B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
- B29C48/80—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling at the plasticising zone, e.g. by heating cylinders
- B29C48/83—Heating or cooling the cylinders
- B29C48/832—Heating
-
- 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
- B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
- B29C48/875—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling for achieving a non-uniform temperature distribution, e.g. using barrels having both cooling and heating zones
-
- 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
- B29C48/92—Measuring, controlling or regulating
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92009—Measured parameter
- B29C2948/92209—Temperature
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92504—Controlled parameter
- B29C2948/9258—Velocity
- B29C2948/9259—Angular velocity
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92504—Controlled parameter
- B29C2948/92704—Temperature
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92819—Location or phase of control
- B29C2948/92857—Extrusion unit
- B29C2948/92876—Feeding, melting, plasticising or pumping zones, e.g. the melt itself
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92819—Location or phase of control
- B29C2948/92857—Extrusion unit
- B29C2948/92876—Feeding, melting, plasticising or pumping zones, e.g. the melt itself
- B29C2948/92885—Screw or gear
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92819—Location or phase of control
- B29C2948/92857—Extrusion unit
- B29C2948/92876—Feeding, melting, plasticising or pumping zones, e.g. the melt itself
- B29C2948/92895—Barrel or housing
-
- 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
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
- Processes Specially Adapted For Manufacturing Cables (AREA)
Description
この発明は、押出機などのプラスチツク成形機
を用いてプラスチツクを成形する際、成形機内の
樹脂温度を成形に最適な温度に制御するためのプ
ラスチツク成形機における樹脂温度制御方法に関
する。
プラスチツクの押出成形などにおいて、押出機
のシリンダ内の各ゾーンの樹脂温度を使用樹脂に
適した温度に制御することは、押出量の増加，ス
コーチの減少，エネルギーコストの低減などの点
から非常に重要な意味を有している。
従来の押出機の樹脂温度制御は、第１図に示す
ように、押出機１のシリンダ２にシリンダ２を貫
通しない複数の測温穴３…を穿設し、この測温穴
３…に測温素子４…を差し込み、シリンダ２の供
給ゾーン，圧縮ゾーン，計量ゾーンの各ゾーンの
温度を測定し、これらの温度を温度調節計５…に
入力し、シリンダ２の外側に設けられたバンドヒ
ータ（或いはアルミ鋳込みヒーター）６…および
冷却ブロア７…をこれら温度調節計５…で制御さ
せる方法によつて行われていた。
しかし、最近の研究によればこの方法には、次
の問題があることが明らかになつた。押出機１
内部が空のときの押出機１の周囲の室温の変化に
より、シリンダ２内面の温度とシリンダ２の温度
との間には第２図に示したような温度差（Δ
T1）が各ゾーン毎に発生する。押出機１中に樹
脂を流したときの押出機１のスクリユ８の回転数
の変化によつて第３図に示したような実際の樹脂
温度とシリンダ２の温度との温度差が更にΔT2
分だけ増加する。したがつて、これらの影響によ
つて、シリンダ２内の溶融樹脂の温度は適正温度
以上に加熱された状態となつており、無駄なエネ
ルギーを消費していたことが判明した。なお、第
２図および第３図中のC2，C3，C4は、シリンダ
２の測温位置を表わすもので、第１図中の各温度
調節計５…に示されているC2，C3，C4の各ゾー
ンに対応している。（ただしC1の位置は直接溶融
に係るものではないからかならずしも本発明によ
る精密な温度調節は必要ではない。もちろんこの
位置での温調を行なつてもさしつかえないが、本
発明の例では従来方式にとどめてある。）
このため、第４図に示されるように、シリンダ
２にこれを貫通する測温孔９…を穿設し、この測
温孔９に測温素子４を溶融樹脂に直接接触するよ
うに差し込み、各ゾーンの溶融樹脂温度を直接測
定し、この温度に基づいて樹脂温度を制御する方
法が考えられている。しかしながら、この方法で
は、シリンダ２にこれを貫通する測温孔９…を穿
設するため、シリンダ２の機械的強度の低下の恐
れがあり、また測温孔９によつてシリンダ２内の
樹脂の流れに乱れが生じ押出製品に悪影響を与え
たり、シリンダ２内の樹脂圧力が高い圧縮ゾー
ン，計量ゾーンでは測温孔９内に樹脂が侵入する
ことがあり、これを防止するためのシールに手間
を要するなどの欠点がある。
この発明は上記事情に鑑みてなされたもので、
押出機などのシリンダ内の樹脂の温度を、常に最
適な温度に保つことができ、吐出量の増大，スコ
ーチの減少，エネルギー節約が計られ、高品質の
成形品を得ることのできるプラスチツク成形機に
おける樹脂温度制御方法を提供することを目的と
し、シリンダの温度を測定しこの温度に、室温，
スクリユ回転数などの溶融樹脂温度を変化させる
パラメータから算出された温度を補正してシリン
ダ内の溶融樹脂温度を予測し、この予測樹脂温度
と希望樹脂温度との偏差を求め、この偏差に基づ
いてシリンダ内の溶融樹脂温度を制御することを
特徴とするものである。
以下、図面を参照してこの発明を詳しく説明す
る。
第５図はこの発明の温度制御方法を適用して温
度制御される押出機の構成例を示すもので、第１
図と同一構成部分には同一符号を付してその説明
を省略する。押出機１のシリンダ２の各ゾーンに
は、このシリンダ２の各ゾーンの温度を測定する
熱電対C1，C2，C3，C4が設けられている。これ
ら熱電対Ｃは第６図に示すように、シリンダ２の
内表面から約10mm程度の厚みを残して穿設された
測温穴３…に挿入されている。なお、測温穴３…
の深さは、押出機１や押出条件等を考慮して選定
するのが良い。また、スクリユ８の基部には、こ
のスクリユ８の回転数を検出する回転発電機１０
が取り付けられ、さらに押出機１の周囲の室温を
測定する測温抵抗体１１が設けられている。そし
て、これら熱電対Ｃ，回転発電機１０および測温
抵抗体１１からの出力は、第７図に示されたこの
発明の温度制御方法に好適な処理システムに送ら
れる。すなわち、熱電対C2，C3，C4および室温
測温抵抗体１１からの出力信号はリニアライザ１
２…に入力され、リニアライズされる。そして、
このリニアライズされた信号はスキヤナ１３に送
られ、スキヤナ１３で、マイクロプロセツサ１４
からのスキヤン指令に基づいて、順次Ａ／Ｄ変換
器１５に入力され、デイジタル化され、さらにマ
イクロプロセツサ１４に入力される。また、スク
リユ回転発電機１０からの信号は、別のＡ／Ｄ変
換器１６に入力されてデイジタル化され、マイク
ロプロセツサ１４に入力される。
マイクロプロセツサ１４では、予じめメモリさ
れた第２図および第３図の室温と△T1との関係
およびスクリユ回転数と△T2との関係に基づ
き、その室温とスクリユ回転数とから、各測温位
置における△T1と△T2を演算し、これら△T1と
△T2に熱電対C2，C3，C4で測定されたシリンダ
２の温度を加算し、シリンダ２内の樹脂温度を各
ゾーン毎に予測する。そしてこれらの予測樹脂温
度と予じめメモリーされた希望樹脂温度との偏差
を演算し、この偏差に基づいて各温度調節計１９
へ新しい設定温度がマイクロプロセツサ１４から
出力側のスキヤナ１７に送られ、マイクロプロセ
ツサ１４からのスキヤン指令に基づいて、順次
Ｄ／Ａ変換器１８…に送られる。この際、各ゾー
ンの新しい設定温度は、そのゾーンに対応して設
けられたＤ／Ａ変換器１８に入力され、アナログ
化され、さらに各ゾーンに対応して設けられた温
度調節計１９…に送られる。また、この設定温度
は、熱電対C2，C3，C4からの信号を参考にして
マイクロプロセツサ１４が定めたタイミングに従
つて温度調節計１９…に送られる。温度調節計１
９…は、上述のようにして指令された新しい設定
温度に基づいて、各ゾーンに対応して設けられた
ヒータ２０…、ブロア２１…の動作を制御し、シ
リンダ２内の樹脂の温度を希望樹脂温度となるよ
うに制御する。
このような温度制御方法によれば、シリンダ２
内の樹脂の樹脂温度に影響を与えるスクリユ８の
回転数および押出機１の周囲の室温が変化して
も、この変化に伴つて生ずる樹脂温度の変動量が
マイクロプロセツサ１４にて直ちに求められ、常
にこの変動量が加味された新しい設定温度によつ
て、樹脂温度が制御されるので、シリンダ２内の
樹脂の樹脂温度は、常に適正な温度に保もたれ
る。
なお、以上説明した例では、樹脂温度に影響を
与える代表的なパラメータとして室温とスクリユ
回転数を選び、これらパラメータによつて樹脂温
度を予想したが、パラメータとして、他の要素、
すなわちヒータ２０，ブロア２１の容量，シリン
ダ２の熱容量，樹脂の種類などをも考慮すればよ
り一層正確に樹脂温度を制御することが可能であ
る。さらには、温調の為のゾーンをより多くする
ことによつてより正確な樹脂温度を予測し、これ
によつて最適な温度制御が可能となり、さらにま
た各ゾーンにおける例えばヒーター２０…を多数
の分割方式とすることによつてもよりよい温度制
御が可能なばかりでなく、エネルギーロスも最小
限とすることができる。さらに、上記の例では、
押出機１の測温ゾーンに対応する熱電対C2，
C3，C4についてのみ本発明に係る温度制御方法
を適用しているが、ホツパー側の測温ゾーンに対
応する熱電対C1についても同様にこの温度制御
方法を適用してもよい。しかし、通常の押出作業
ではC2，C3，C4の三ゾーンの温度制御で充分で
ある。また、シリンダ２の加熱、冷却手段も上記
例に限られることなく、例えばシリコーン油など
の流体熱媒を用いた加熱、冷却手段を用いてもよ
い。
以下、実施例を示して、具体的に説明する。
〔実施例〕
スクリユ径50mm、Ｌ／Ｄ＝20、シリンダ肉厚25
mm、ヒータ容量C12.2KW、C2，C3，C40.7KW、
PID温度調節計付き押出機を用い、本発明の温度
制御方法を適用して架橋剤入り低密度ポリエチレ
ンを押出成形した。
(1) 設定温度
熱電対をシリンダ内表面から10mmの距離に配置
して、
C1……120℃固定とし
C2，C3，C4……マイクロプロセツサからの指
令による。
(2) 各ゾーンの希望樹脂温度Ｅ
The present invention relates to a resin temperature control method in a plastic molding machine for controlling the resin temperature in the molding machine to an optimal temperature for molding when plastic is molded using a plastic molding machine such as an extruder. In plastic extrusion molding, etc., controlling the resin temperature in each zone in the extruder cylinder to a temperature suitable for the resin used is extremely important in terms of increasing extrusion volume, reducing scorch, and reducing energy costs. It has important meaning. As shown in Fig. 1, conventional extruder resin temperature control involves drilling a plurality of temperature measuring holes 3 in the cylinder 2 of the extruder 1, which do not penetrate the cylinder 2, and inserting the temperature into the temperature measuring holes 3. Insert the temperature element 4... to measure the temperature of each zone of the cylinder 2, including the supply zone, compression zone, and metering zone.These temperatures are input to the temperature controller 5..., and the band heater installed outside the cylinder 2 is heated. (or an aluminum casting heater) 6... and a cooling blower 7... are controlled by these temperature controllers 5.... However, recent research has revealed that this method has the following problems. Extruder 1
Due to changes in the room temperature around the extruder 1 when the inside is empty, there is a temperature difference (Δ) between the temperature of the inner surface of the cylinder 2 and the temperature of the cylinder 2 as shown in
T 1 ) occurs in each zone. Due to the change in the rotational speed of the screw 8 of the extruder 1 when the resin is poured into the extruder 1, the temperature difference between the actual resin temperature and the temperature of the cylinder 2 as shown in FIG. 3 further increases by ΔT 2
increase by the amount. Therefore, it was found that due to these influences, the temperature of the molten resin in the cylinder 2 was heated to a temperature higher than the appropriate temperature, and energy was wasted. Note that C 2 , C 3 , and C 4 in FIGS. 2 and 3 represent the temperature measurement positions of the cylinder 2, and C 2 shown in each temperature controller 5 in FIG. , C 3 , and C 4 zones. (However, since the position C1 is not directly related to melting, precise temperature control according to the present invention is not necessarily necessary.Of course, temperature control at this position is fine, but in the example of the present invention, For this reason, as shown in Fig. 4, a temperature measuring hole 9 is drilled through the cylinder 2, and the temperature measuring element 4 is placed in the molten resin in the temperature measuring hole 9. A method has been considered in which the temperature of the molten resin in each zone is directly measured by inserting the resin into direct contact with each other, and the resin temperature is controlled based on this temperature. However, in this method, the temperature measuring holes 9 are bored through the cylinder 2, so there is a risk of a decrease in the mechanical strength of the cylinder 2. turbulence in the flow may adversely affect the extruded product, or resin may enter the temperature measurement hole 9 in the compression zone and metering zone where the resin pressure inside the cylinder 2 is high. It has drawbacks such as being time consuming. This invention was made in view of the above circumstances,
A plastic molding machine that can always keep the temperature of the resin in the cylinder of an extruder at the optimum temperature, increasing the discharge amount, reducing scorch, saving energy, and producing high-quality molded products. The purpose is to provide a resin temperature control method in which the temperature of the cylinder is measured and this temperature is adjusted to room temperature,
The temperature calculated from parameters that change the molten resin temperature, such as the screw rotation speed, is corrected to predict the molten resin temperature in the cylinder, the deviation between this predicted resin temperature and the desired resin temperature is determined, and based on this deviation, It is characterized by controlling the temperature of the molten resin inside the cylinder. Hereinafter, the present invention will be explained in detail with reference to the drawings. FIG. 5 shows an example of the configuration of an extruder whose temperature is controlled by applying the temperature control method of the present invention.
Components that are the same as those in the figures are given the same reference numerals and their explanations will be omitted. Each zone of the cylinder 2 of the extruder 1 is provided with thermocouples C 1 , C 2 , C 3 , and C 4 for measuring the temperature of each zone of the cylinder 2. As shown in FIG. 6, these thermocouples C are inserted into temperature measuring holes 3 bored from the inner surface of the cylinder 2 leaving a thickness of about 10 mm. In addition, temperature measurement hole 3...
The depth is preferably selected in consideration of the extruder 1, extrusion conditions, etc. Further, at the base of the screw 8, there is a rotary generator 10 for detecting the rotation speed of the screw 8.
is attached, and furthermore, a resistance temperature detector 11 for measuring the room temperature around the extruder 1 is provided. The outputs from the thermocouple C, rotary generator 10, and resistance temperature detector 11 are sent to a processing system suitable for the temperature control method of the present invention shown in FIG. That is, the output signals from the thermocouples C 2 , C 3 , C 4 and the room temperature resistance thermometer 11 are sent to the linearizer 1.
2... and linearized. and,
This linearized signal is sent to the scanner 13, and the scanner 13 sends it to the microprocessor 14.
Based on a scan command from , the data is sequentially input to the A/D converter 15 , digitized, and further input to the microprocessor 14 . Further, the signal from the screw rotating generator 10 is input to another A/D converter 16, digitized, and input to the microprocessor 14. The microprocessor 14 calculates the temperature from the room temperature and the screw rotation speed based on the relationship between the room temperature and △T 1 and the relationship between the screw rotation speed and △T 2 shown in FIGS. 2 and 3 which are stored in advance. , calculate △T 1 and △T 2 at each temperature measurement position, add the temperature of cylinder 2 measured by thermocouples C 2 , C 3 , and C 4 to these △T 1 and △T 2 , and calculate the temperature of cylinder 2. Predict the temperature of the resin in each zone. Then, the deviation between these predicted resin temperatures and the desired resin temperature stored in advance is calculated, and each temperature controller 19 is adjusted based on this deviation.
A new set temperature is sent from the microprocessor 14 to the scanner 17 on the output side, and based on the scan command from the microprocessor 14, it is sequentially sent to the D/A converters 18 . At this time, the new set temperature for each zone is input to the D/A converter 18 provided corresponding to that zone, converted to analog, and then sent to the temperature controller 19 provided corresponding to each zone. Sent. Further, this set temperature is sent to the temperature controllers 19 in accordance with the timing determined by the microprocessor 14 with reference to the signals from the thermocouples C 2 , C 3 , and C 4 . Temperature controller 1
9... controls the operation of the heater 20..., blower 21... provided corresponding to each zone based on the new set temperature commanded as described above, and sets the desired temperature of the resin in the cylinder 2. Control the resin temperature. According to such a temperature control method, the cylinder 2
Even if the rotational speed of the screw 8 and the room temperature around the extruder 1, which affect the temperature of the resin inside the extruder 1, change, the microprocessor 14 immediately determines the amount of variation in the resin temperature that occurs due to these changes. Since the resin temperature is always controlled using a new set temperature that takes this amount of variation into account, the resin temperature of the resin in the cylinder 2 is always maintained at an appropriate temperature. In the example explained above, room temperature and screw rotation speed were selected as typical parameters that affect resin temperature, and resin temperature was predicted based on these parameters. However, other factors such as
That is, if the capacities of the heater 20 and blower 21, the heat capacity of the cylinder 2, the type of resin, etc. are taken into consideration, it is possible to control the resin temperature even more accurately. Furthermore, by increasing the number of zones for temperature control, it is possible to predict the resin temperature more accurately, thereby making it possible to perform optimal temperature control. By using the split method, not only better temperature control is possible, but also energy loss can be minimized. Additionally, in the example above,
Thermocouple C 2 corresponding to the temperature measurement zone of extruder 1,
Although the temperature control method according to the present invention is applied only to C 3 and C 4 , this temperature control method may be similarly applied to thermocouple C 1 corresponding to the temperature measurement zone on the hopper side. However, in normal extrusion operations, temperature control in three zones, C2 , C3 , and C4 , is sufficient. Further, the means for heating and cooling the cylinder 2 is not limited to the above example, and heating and cooling means using a fluid heat medium such as silicone oil may also be used. Hereinafter, a specific explanation will be given by showing examples. [Example] Screw diameter 50mm, L/D=20, cylinder wall thickness 25
mm, heater capacity C 1 2.2KW, C 2 , C 3 , C 4 0.7KW,
A crosslinking agent-containing low density polyethylene was extruded using an extruder equipped with a PID temperature controller and applying the temperature control method of the present invention. (1) Temperature setting Place the thermocouple at a distance of 10 mm from the inner surface of the cylinder, C 1 ... fixed at 120°C, C 2 , C 3 , C 4 ... based on commands from the microprocessor. (2) Desired resin temperature E for each zone
【表】
(3) 樹脂温度予測式
Ｙ＝ｙ＋△T1＋△T2
Ｙ：予測樹脂温度
ｙ：熱電対Ｃによるシリンダの温度
△T1：室温による補正温度
△T2：スクリユ回転数による補正温度
(4) 制御方法
次式によつて新しい設定温度を演算して温度調
節計１９へ指令する方式とする。
新設定温度＝現在の設定温度−（Ｙ−Ｅ）×0.9
上式におけるフアクタ0.9は希望樹脂温度に実
際樹脂温度を低目から漸近させるようにしたもの
で、１でもよいが１では希望樹脂温度をオーバす
ることがある。
以上の条件下で、スクリユ回転数を30rpm、
60rpm、70rpmと変化させて実際樹脂温度Ａを測
定し、希望樹脂温度Ｅとの差を比較した。第１表
は、押出開始後、２〜４回の設定温度変更指令の
後の各ゾーンのシリンダの温度ｙ、予測樹脂温度
Ｙ、実際樹脂温度Ａ、希望樹脂温度Ｅ、およびＡ
−Ｅを示す。
なお、実際樹脂温度Ａはシリンダの各ゾーンに
貫通孔を穿設して、測温素子を溶融樹脂に接触す
るまで挿入して測定した。[Table] (3) Resin temperature prediction formula Y = y + △T 1 + △T 2 Y: Predicted resin temperature y: Cylinder temperature determined by thermocouple C △T 1 : Temperature corrected by room temperature △T 2 : Depends on screw rotation speed Corrected temperature (4) Control method A new set temperature is calculated using the following formula and commanded to the temperature controller 19. New set temperature = Current set temperature - (Y-E) x 0.9 The factor 0.9 in the above equation is to make the actual resin temperature asymptotically approach the desired resin temperature from a low value, and it may be 1, but 1 is the desired resin temperature. may exceed. Under the above conditions, the screw rotation speed was set to 30 rpm.
The actual resin temperature A was measured by changing the rpm to 60 rpm and 70 rpm, and the difference with the desired resin temperature E was compared. Table 1 shows the cylinder temperature y, predicted resin temperature Y, actual resin temperature A, desired resin temperature E, and A of each zone after two to four set temperature change commands after the start of extrusion.
- indicates E. The actual resin temperature A was measured by drilling a through hole in each zone of the cylinder and inserting a temperature measuring element until it came into contact with the molten resin.
【表】
第１表より実際樹脂温度Ａと希望樹脂温度Ｅと
の偏差｜Ａ−Ｅ｜は、最高でも約4.5℃であり、
後述する従来方式に比べて大幅に温度偏差が少な
くなつている。
次に、従来の温度制御法を適用した従来例を示
す。
〔従来例〕
実施例の押出機と同一の押出機を用い、温度調
節に通常のPID式温度調節計を用いて、各ゾーン
を120℃に調節した以外は実施例と同様にして押
出作業を行つた。第２表に、シリンダの温度ｙ、
実際樹脂温度Ａ、希望樹脂温度Ｅ、およびＡ−Ｅ
を示した。[Table] From Table 1, the deviation between the actual resin temperature A and the desired resin temperature E |A-E| is approximately 4.5℃ at maximum.
The temperature deviation is significantly reduced compared to the conventional method described later. Next, a conventional example to which a conventional temperature control method is applied will be shown. [Conventional example] Extrusion work was carried out in the same manner as in the example except that the same extruder as in the example was used, a normal PID temperature controller was used for temperature control, and each zone was adjusted to 120°C. I went. Table 2 shows the cylinder temperature y,
Actual resin temperature A, desired resin temperature E, and A-E
showed that.
【表】
第２表から、実際樹脂温度Ａと希望樹脂温度Ｅ
との偏差｜Ａ−Ｅ｜が最高で約８℃となることが
わかる。なお、この値はスクリユー回転数を更に
上げた場合には偏差（Ａ−Ｅ）が10℃以上にもな
ることがある。このような大きな温度偏差がある
状態では押出成形品の品質上種々の問題が生じ
る。
以上説明したように、この発明のプラスチツク
成形機における樹脂温度制御方法は、プラスチツ
ク成形機のシリンダの温度を測定し、この温度に
室温，スクリユ回転数など樹脂温度を変動させる
パラメータから算出された温度を補正してシリン
ダ内の樹脂温度を予測し、この予測温度と希望樹
脂温度との偏差を求め、この偏差に基づいて樹脂
温度を制御するものである。したがつて、この温
度制御方法によれば、室温やスクリユ回転数が変
化しても、常に正確な樹脂温度を予測でき、これ
によつて実際の樹脂温度を最適に制御できるの
で、吐出量の向上，スコーチの減少，熱エネルギ
ーの節約が計られ、高品質の成形品を低コストで
製造できる。また、シリンダ内の樹脂の温度を直
接測定する方式に比べて、シリンダを貫通する測
温孔などを設ける必要がなく、シリンダの強度が
高く保たれ、シリンダ内の樹脂の流れに乱れが生
じず、さらに測温孔に樹脂が侵入することがな
く、シールなどの手間が不要になるなどの利点を
も有している。よつて、この温度制御方法は、一
般のスクリユータイプの押出機は勿論の事、スク
リユータイプの射出成形機などのプラスチツク成
形機に広く応用できる。[Table] From Table 2, the actual resin temperature A and the desired resin temperature E
It can be seen that the deviation |A−E| from the maximum value is about 8°C. Note that when the screw rotation speed is further increased, the deviation (A-E) of this value may exceed 10°C. When there is such a large temperature deviation, various problems arise in terms of the quality of the extruded product. As explained above, the resin temperature control method in the plastic molding machine of the present invention measures the temperature of the cylinder of the plastic molding machine, and adds a temperature calculated from parameters that vary the resin temperature, such as room temperature and screw rotation speed, to this temperature. is corrected to predict the resin temperature in the cylinder, the deviation between this predicted temperature and the desired resin temperature is determined, and the resin temperature is controlled based on this deviation. Therefore, according to this temperature control method, even if the room temperature or the screw rotation speed changes, the resin temperature can always be accurately predicted, and the actual resin temperature can thereby be optimally controlled, thereby reducing the discharge amount. improved performance, reduced scorch, and saved thermal energy, allowing high-quality molded products to be produced at low cost. In addition, compared to methods that directly measure the temperature of the resin inside the cylinder, there is no need to provide a temperature measurement hole penetrating the cylinder, the strength of the cylinder is maintained high, and there is no disturbance in the flow of resin inside the cylinder. Furthermore, it has the advantage that resin does not enter the temperature measurement hole, and there is no need for sealing or other labor. Therefore, this temperature control method can be widely applied to plastic molding machines such as screw type injection molding machines as well as general screw type extruders.
第１図は、従来の温度制御方法を適用した押出
機を示す概略構成図、第２図は室温の変化と△
T1との関係を示すグラフ、第３図はスクリユ回
転数の変化と△T2との関係を示すグラフ、第４
図は樹脂温度直接測定方式の測温素子の取付状態
を示す概略断面図、第５図はこの発明の温度制御
方法を適用した押出機の一例を示す概略構成図、
第６図はこの発明の温度制御方法に採用される測
温素子の取付状態を示す概略断面図、第７図はこ
の発明の温度制御方法に用いられる制御システム
の一例を示すブロツク図である。
１……押出機、２……シリンダ、３……測温
穴、８……スクリユ、C2，C3，C4……熱電対、
１０……回転発電機、１１……測温抵抗体、１２
……リニアライザ、１３……スキヤナ、１４……
マイクロプロセツサ、１５，１６……Ａ／Ｄ変換
器、１７……スキヤナ、１８……Ｄ／Ａ変換器、
１９……温度調節計、２０……ヒータ、２１……
ブロア。
Figure 1 is a schematic configuration diagram showing an extruder using a conventional temperature control method, and Figure 2 shows changes in room temperature and △
Figure 3 is a graph showing the relationship between T 1 and △T 2. Figure 4 is a graph showing the relationship between changes in screw rotation speed and ΔT 2 .
The figure is a schematic cross-sectional view showing the mounting state of the thermometer element of the resin temperature direct measurement method, and FIG. 5 is a schematic configuration diagram showing an example of an extruder to which the temperature control method of the present invention is applied.
FIG. 6 is a schematic sectional view showing the mounting state of the temperature measuring element employed in the temperature control method of the present invention, and FIG. 7 is a block diagram showing an example of a control system used in the temperature control method of the present invention. 1...Extruder, 2...Cylinder, 3...Temperature measuring hole, 8...Screw, C2 , C3 , C4 ...Thermocouple,
10... Rotating generator, 11... Resistance temperature detector, 12
...Linearizer, 13...Sukiyana, 14...
Microprocessor, 15, 16...A/D converter, 17...Scanner, 18...D/A converter,
19... Temperature controller, 20... Heater, 21...
Blower.
Claims (1)
し、この温度に室温、スクリユ回転数などの溶融
樹脂温度を変動させるパラメータから算出された
温度を補正してシリンダ内の溶融樹脂温度を予測
し、この予測樹脂温度と希望樹脂温度との偏差を
求め、この偏差に基づいてシリンダ内の溶融樹脂
の温度を制御することを特徴とするプラスチツク
成形機の樹脂温度制御方法。1 Measure the temperature of the cylinder of the plastic molding machine, correct the temperature calculated from parameters that vary the molten resin temperature, such as room temperature and screw rotation speed, to predict the molten resin temperature in the cylinder, and use this prediction. A resin temperature control method for a plastic molding machine, characterized in that a deviation between a resin temperature and a desired resin temperature is determined, and the temperature of molten resin in a cylinder is controlled based on this deviation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56191906A JPS58108119A (en) | 1981-11-30 | 1981-11-30 | Controlling method for temperature of resin in plastic molding machine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56191906A JPS58108119A (en) | 1981-11-30 | 1981-11-30 | Controlling method for temperature of resin in plastic molding machine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58108119A JPS58108119A (en) | 1983-06-28 |
| JPS6149094B2 true JPS6149094B2 (en) | 1986-10-28 |
Family
ID=16282410
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56191906A Granted JPS58108119A (en) | 1981-11-30 | 1981-11-30 | Controlling method for temperature of resin in plastic molding machine |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58108119A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58148740A (en) * | 1982-02-27 | 1983-09-03 | Fujikura Ltd | Controlling method for resin temperature at plastic molding machine |
| JPS6237122A (en) * | 1985-08-12 | 1987-02-18 | Hitachi Cable Ltd | Controller of cylinder temperature of chemical foam extruding machine |
| DE3623679A1 (en) * | 1986-07-12 | 1988-01-28 | Werner & Pfleiderer | METHOD FOR OPERATING A SNAIL EXTRUDER AND SNAIL EXTRUDER FOR IMPLEMENTING THE METHOD |
-
1981
- 1981-11-30 JP JP56191906A patent/JPS58108119A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58108119A (en) | 1983-06-28 |
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