JP2527465B2 - Membrane production equipment - Google Patents
Membrane production equipmentInfo
- Publication number
- JP2527465B2 JP2527465B2 JP63167159A JP16715988A JP2527465B2 JP 2527465 B2 JP2527465 B2 JP 2527465B2 JP 63167159 A JP63167159 A JP 63167159A JP 16715988 A JP16715988 A JP 16715988A JP 2527465 B2 JP2527465 B2 JP 2527465B2
- Authority
- JP
- Japan
- Prior art keywords
- coagulation
- solvent
- liquid
- enclosure
- polymer solution
- 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 - Fee Related
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Artificial Filaments (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、相変換法による膜製造装置に関するもので
ある。DETAILED DESCRIPTION OF THE INVENTION [Industrial field of use] The present invention relates to a film production apparatus by a phase conversion method.
膜を形成するポリマー溶液を中空糸状、管状あるいは
平板状に整形して非溶媒中で凝固させる相変換法による
製膜法において、凝固液として用いる非溶媒の種類、組
成は膜構造、膜性能に大きく影響する重要な因子であ
る。例えば、水を非溶媒として使用する場合と、ポリマ
ー溶液を構成する溶剤又は溶剤組成の一部を加えた水溶
液を非溶媒として使用する場合とを比べると、膜構造及
び膜性能が異なり、水に溶剤等を加えることにより凝固
液の凝固価を調整し、以て相変換時の溶剤、非溶剤の移
動、ゲルの成長を制御することによって、より性能のよ
い膜を得ることができる場合がある。In the film forming method by the phase conversion method in which the polymer solution forming the film is shaped into a hollow fiber, a tube or a flat plate and coagulated in a non-solvent, the type and composition of the non-solvent used as the coagulating liquid depend on the film structure and film performance. It is an important factor that has a great influence. For example, comparing the case where water is used as a non-solvent and the case where an aqueous solution obtained by adding a part of a solvent or a solvent composition constituting a polymer solution is used as a non-solvent, the membrane structure and the membrane performance are different, and By adjusting the coagulation value of the coagulation liquid by adding a solvent, etc., it may be possible to obtain a film with better performance by controlling the migration of the solvent and non-solvent during phase conversion and the growth of gel. .
しかしながら、凝固液の量は、ポリマー溶液量に比
し、桁違いに大きいため、水以外の比溶媒を使用するこ
とはたとえ水溶液であっても、経費負担と廃液処理負荷
が大きい。このため、工業生産における凝固液として用
いられる非溶媒は実質的に水に限定されている。However, the amount of the coagulating liquid is incomparably larger than the amount of the polymer solution, and therefore the use of a specific solvent other than water, even if it is an aqueous solution, imposes a large cost burden and a large waste liquid treatment load. Therefore, the non-solvent used as the coagulating liquid in industrial production is substantially limited to water.
本発明は、凝固槽内非溶媒に溶媒及び／又は添加剤を
加え、而も上記の如く経費、廃液処理両負担を実質的に
増大させることなしに相当する効果を生ぜしめ、相変換
法により優れた膜性能を有する膜を得る膜製造装置を提
供するものである。The present invention adds a solvent and / or an additive to the non-solvent in the coagulation tank, and produces a corresponding effect without substantially increasing both the cost and the waste liquid treatment load as described above, and the phase conversion method is used. It is intended to provide a film production apparatus for obtaining a film having excellent film performance.
本発明者等は、ポリマー溶液が非溶媒中で凝固する際
に非溶媒の性質が膜構造の決定に及ぼす効果が最も大き
いのは、両者が接触する期間のうち、最初の短期間であ
ることに着目して、凝固槽の全非溶媒を均一な組成にす
る必要がないことに想到した。即ち、凝固槽をポリマー
溶液が非溶媒に最初に接触する第一の凝固部と初期表面
硬化したポリマー溶液が通過する第二の凝固部とから構
成する。第一の凝固部は少なくとも最初の凝固液を水の
代わりに溶剤水溶液等にして、その凝固価を望ましい値
に調整すれば、使用溶剤量を減らして溶剤含有による実
効を得ることができる。この様に凝固槽を複数の凝固部
に分割することの利点は、上述の単純な比例計算以上の
ものがある。即ち、大多数の製膜用ポリマー溶液に対し
て、水は凝固価の最も小さい（即ち凝固力の最も強い）
非溶剤であり、相変換に必要な凝固液としては少量で済
む。これに対し、有機非溶剤や溶剤水溶液の凝固価は水
よりも大きく、一般に相変換を完了するのにより長時間
を要する。従って、凝固槽を分割しない場合は凝固液と
して水を用いる場合よりも一層大量を必要とするが、凝
固槽を分割して、前段にのみ凝固価のより大きい凝固液
を用い、後段の凝固液の凝固価を小さくすることによ
り、この問題を回避乃至軽減することができる。一方、
凝固槽内のポリマー溶液からは溶剤、添加剤又は溶剤及
び芯液が製膜速度、即ち、ポリマー溶液が凝固槽内に吐
出される速度に応じた一定速度で非溶媒中に溶出してく
る。この溶剤、添加剤等の量は、凝固液量に比し僅かで
あるが、製膜を長時間連続して行うと、非溶媒からなる
凝固液中の濃度が上昇し続けるため、これによる凝固液
の凝固価の経時変化は長時間に亘ってみれば無視できな
くなる。この変動を防ぐため、通常は連続して凝固液の
一部排出と水の補給とを行い、凝固液中の溶剤濃度を低
く保っている。しかるに、凝固液量を、例えば通常の10
-3〜10-4と極度に少量にすることができれば、整形され
たポリマー溶液から凝固液中に移行した溶剤、添加剤等
の濃度は短時間で上昇するため、同様の操作によって凝
固液中の溶剤濃度を十分広範囲に調整、維持できること
に想到した。更に、凝固液の凝固価を調整するために加
える溶剤、添加剤としては、製膜用ポリマー溶液に使用
するものと同じ溶剤、添加剤で良好な結果を得ることが
できる。これらの知見を併せ考慮することにより、本発
明に到った。The inventors of the present invention have found that the effect of the property of the non-solvent on the determination of the film structure when the polymer solution is solidified in the non-solvent is that the contact period between the two is the first short period. Focusing on, we came to the idea that it is not necessary to make all the non-solvents in the coagulation tank a uniform composition. That is, the coagulation tank is composed of a first coagulation part in which the polymer solution first comes into contact with the non-solvent and a second coagulation part in which the polymer solution whose initial surface is hardened passes through. In the first coagulation unit, at least the first coagulation liquid is replaced with water by using a solvent aqueous solution or the like, and the coagulation value thereof is adjusted to a desired value, so that the amount of solvent used can be reduced and the effect of containing the solvent can be obtained. The advantage of dividing the coagulation tank into a plurality of coagulation portions in this manner is more than the simple proportional calculation described above. That is, water has the smallest coagulation value (that is, the strongest coagulation power) with respect to the majority of polymer solutions for film formation.
It is a non-solvent and requires only a small amount of coagulation liquid for phase conversion. On the other hand, the solidification number of the organic non-solvent or the aqueous solution of the solvent is larger than that of water, and it generally takes a longer time to complete the phase conversion. Therefore, when the coagulation tank is not divided, a larger amount is required than when water is used as the coagulation liquid, but the coagulation tank is divided and the coagulation liquid having a larger coagulation value is used only in the first stage and the coagulation liquid in the latter stage is used. This problem can be avoided or alleviated by reducing the coagulation value of the. on the other hand,
From the polymer solution in the coagulation tank, the solvent, the additive or the solvent and the core liquid are eluted into the non-solvent at a constant rate according to the film forming speed, that is, the speed at which the polymer solution is discharged into the coagulation tank. The amount of this solvent, additive, etc. is small compared to the amount of coagulation liquid, but if film formation is continuously performed for a long time, the concentration in the non-solvent coagulation liquid will continue to rise, so the coagulation by this The change with time of the coagulation value of the liquid cannot be ignored over a long period of time. In order to prevent this fluctuation, normally, the coagulation liquid is partially discharged and water is replenished continuously to keep the solvent concentration in the coagulation liquid low. However, the amount of coagulation liquid is, for example, 10
-3 to 10 -4 If the amount can be made extremely small, the concentration of the solvent, additives, etc. transferred from the shaped polymer solution into the coagulation liquid will rise in a short time. It was thought that the solvent concentration of could be adjusted and maintained in a sufficiently wide range. Further, as the solvent and the additive added for adjusting the coagulation value of the coagulating liquid, the same solvent and additive as those used for the polymer solution for film formation can be used to obtain good results. The present invention has been accomplished by taking these findings into consideration.
即ち、本発明は高分子溶液を整形するノズル部及び非
溶媒からなる凝固液を充填する凝固槽を有し、凝固槽内
の凝固部に整形した高分子溶液の流れに沿う様にある距
離を隔てて囲いが設けられ、囲いの内外の非溶媒からな
る凝固液の凝固価がそれぞれ異なっている相変換法によ
る膜製造装置に於いて、凝固部の囲いの上部又は下部の
いずれか一方に凝固液の抜き取り部が設けられているこ
とを特徴とする膜製造装置に関するものである。That is, the present invention has a nozzle section for shaping a polymer solution and a coagulation tank filled with a coagulation liquid composed of a non-solvent, and a certain distance is set along the flow of the shaped polymer solution in the coagulation section in the coagulation tank. In a membrane manufacturing device by the phase conversion method, in which the coagulation liquids of the non-solvents inside and outside the enclosure are provided with separate enclosures and the coagulation values are different from each other, the coagulation is either on the upper part or the lower part of the enclosure of the coagulation part. The present invention relates to a film manufacturing apparatus, which is provided with a liquid extracting section.
本発明の膜製造装置に於いては、凝固部の凝固槽内に
於いてポリマー溶液が最初に非溶媒と接触する部分を整
形したポリマー溶液の流れに沿って或る距離囲うことに
よって、この囲いの内側では、非溶媒中の溶剤濃度はポ
リマー溶液からの溶出による増加作用と、囲いの開放部
からの逃散による減少作用とが拮抗して或る平衡濃度に
到達し、その濃度は囲いの寸法、形態、或いは囲いの一
部から非溶媒の一部を抜き出す速度等を変えることによ
って容易に変えることができる。特に、この囲いは整形
されたポリマー溶液の移動方向に沿った細長い形状にす
ることにより、囲いの内容積及び下流側に設けた開放部
面積を共に十分小さくすることができ、囲い内の溶剤濃
度を短時間に平衡濃度に到達させることができる。従っ
て、凝固液はこの囲いによって分割され、囲いの内外に
それぞれ凝固価の異なる非溶媒からなる凝固液が存在す
ることになる。整形されたポリマー溶液は、先ず凝固価
が水よりも高い値に設定された囲い内の第一の凝固液内
を通ることにより、相変換をある程度進行させた後、囲
いの外の実質的には水に近い低凝固価の凝固液を通るこ
とによって相変換を完了する。In the membrane manufacturing apparatus of the present invention, the portion where the polymer solution first comes into contact with the non-solvent in the coagulation tank of the coagulation portion is enclosed by a certain distance along the flow of the shaped polymer solution to form this enclosure. Inside, the solvent concentration in the non-solvent reaches a certain equilibrium concentration by the competing effect of the increasing action due to elution from the polymer solution and the decreasing action due to escape from the open part of the enclosure, which reaches the equilibrium concentration. , The shape, or the rate of extracting a part of the non-solvent from a part of the enclosure can be easily changed. In particular, by making this enclosure elongated along the direction of movement of the shaped polymer solution, both the internal volume of the enclosure and the area of the open part provided on the downstream side can be made sufficiently small, and the solvent concentration in the enclosure can be reduced. Can reach the equilibrium concentration in a short time. Therefore, the coagulation liquid is divided by this enclosure, and the coagulation fluid consisting of nonsolvents having different coagulation values exists inside and outside the enclosure. The shaped polymer solution is first passed through the first coagulating liquid in the enclosure in which the coagulation value is set to a value higher than that of the water, thereby allowing the phase conversion to proceed to some extent, and then substantially outside the enclosure. Completes the phase transformation by passing through a low coagulation liquid that is close to water.
以下、実施態様を図によって説明する。 Embodiments will be described below with reference to the drawings.
図４は従来の乾湿式紡糸で中空糸膜を製膜する装置
を、図１は乾湿式紡糸でポリマー溶液が凝固液と最初に
接触する部分を囲い１で囲った本発明の装置を示す。図
４では、ポリマー溶液から凝固液である非溶媒中に移行
する溶剤は非溶媒中へ自由に拡散するため、ノズルから
中空糸状に押出されたポリマー溶液が接触する非溶媒中
の溶剤濃度は希薄である。これに対し、図１では囲い１
内の非溶媒中に移行した溶剤は囲い１の開口部２を通っ
ての逃散に限定されるため囲い１内の凝固液（以下第一
の凝固液とよぶ）中の溶剤濃度は高くなる。定常状態に
おける溶剤濃度は囲い１内でポリマー溶液から非溶媒へ
移行する溶剤量と囲いの開口部から外部へ拡散する溶剤
量の関係で定まり、これは囲いの長さと開口部面積によ
って変えることができる。FIG. 4 shows a conventional apparatus for forming a hollow fiber membrane by dry-wet spinning, and FIG. 1 shows an apparatus of the present invention in which the portion of the dry-wet spinning at which the polymer solution first comes into contact with the coagulating liquid is surrounded by an enclosure 1. In FIG. 4, the solvent that migrates from the polymer solution into the non-solvent, which is the coagulating liquid, freely diffuses into the non-solvent, so the concentration of the solvent in the non-solvent with which the polymer solution extruded from the nozzle into the hollow fiber shape comes into contact is dilute. Is. On the other hand, in FIG.
The solvent that has migrated to the non-solvent inside is restricted to escape through the opening 2 of the enclosure 1, so that the concentration of the solvent in the coagulating liquid (hereinafter referred to as the first coagulating liquid) in the enclosure 1 becomes high. The solvent concentration in the steady state is determined by the relationship between the amount of solvent that moves from the polymer solution to the non-solvent in the enclosure 1 and the amount of solvent that diffuses from the opening of the enclosure to the outside. This can be changed by the length of the enclosure and the area of the opening. it can.
単純化したモデル計算では囲い内における中空糸状ポ
リマー溶液内の溶剤拡散係数をD1、中空糸表面積をS1、
非溶媒中の溶剤拡散係数をD2、囲いの開口部面積をS2と
して、溶剤濃度は、ポリマー溶液中濃度の に達する。In a simplified model calculation, the solvent diffusion coefficient in the hollow fiber polymer solution in the enclosure is D 1 , the hollow fiber surface area is S 1 ,
Let D 2 be the solvent diffusion coefficient in the non-solvent and S 2 be the opening area of the enclosure. Reach
また、図２はポリマー溶液が非溶媒と最初に接触する
部分を囲った、湿式紡糸による中空糸膜の製膜装置を示
すが、囲い１の上部、即ち紡糸ノズル３の隣接部に凝固
液抜き取り部４を設け、管４′を通して囲い内の非溶媒
を一定流量ｆで外部へ抜き出す場合は、ポリマー溶液か
らの溶剤移行速度をｑとして定常状態の溶剤濃度はq/f
となり、抜き出し速度ｆを変えることによって囲い１内
の第一の凝固液中の溶剤等の濃度をコントロールするこ
とが出来る。この場合凝固液を抜き取る際、抜き取り液
により、囲い１内の液流が乱れるのを防ぐため、乱れの
防止部５を設けるとよい。Further, FIG. 2 shows a hollow fiber membrane forming apparatus by wet spinning in which a portion where the polymer solution first comes into contact with the non-solvent is surrounded, but the coagulation liquid is drawn out at the upper portion of the enclosure 1, that is, adjacent to the spinning nozzle 3. When the portion 4 is provided and the non-solvent in the enclosure is discharged to the outside through the pipe 4'at a constant flow rate f, the solvent transfer rate from the polymer solution is q, and the steady-state solvent concentration is q / f.
Therefore, the concentration of the solvent or the like in the first coagulation liquid in the enclosure 1 can be controlled by changing the extraction speed f. In this case, when the coagulation liquid is drawn out, in order to prevent the liquid flow in the enclosure 1 from being disturbed by the drawing liquid, it is preferable to provide a turbulence prevention unit 5.
本発明の図１及び図２に示した様な囲いを設けた膜製
造装置によれば、この様に凝固槽内の非溶媒に溶剤を全
く加えることなしに、ポリマー溶液から移行してくる溶
剤を巧みに利用することによって多量の溶剤を使うこと
による経費増、廃水処理負荷増なしに、ポリマー溶液
が、非溶媒を最初に接触する部分の非溶媒（第一の凝固
液）中の溶剤濃度を高くコントロールすることが出来、
得られる膜構造、膜性能を制御することができる。According to the membrane manufacturing apparatus provided with the enclosure as shown in FIGS. 1 and 2 of the present invention, the solvent transferred from the polymer solution can be added without adding any solvent to the non-solvent in the coagulation tank. Concentration of solvent in the non-solvent (first coagulation liquid) at the part where the polymer solution comes into contact with the non-solvent first without increasing the cost and load of wastewater treatment by using a large amount of solvent by skillfully utilizing Can be controlled high,
The obtained film structure and film performance can be controlled.
この様に本発明の膜製造装置においては、少なくとも
２種のそれぞれ凝固価の異なる非溶媒からなる凝固液が
分割して配置された凝固部が設けられ、最初に２番目の
凝固液よりも凝固価の大きい非溶媒からなる第一の凝固
液中を通過させるとよい。ここで、凝固価とはポリマー
溶液に濁りを生じさせるに必要な非溶媒の量であり、値
が高い程、凝固力は弱い。As described above, in the film production apparatus of the present invention, the coagulation section in which at least two kinds of coagulation liquids each composed of a non-solvent having a different coagulation value are divided and arranged is provided, and the coagulation liquid is first coagulated more than the second coagulation liquid. It is advisable to pass through a first coagulating liquid consisting of a non-solvent having a high valency. Here, the coagulation number is the amount of the non-solvent required to cause turbidity in the polymer solution, and the higher the value, the weaker the coagulation force.
又、凝固に際しては、図１に示す様に整形高分子溶液
が凝固液に接触する前に、凝固液の蒸発気体部を通過さ
せても（乾湿式紡糸）、図２の様に整形後直ちに凝固液
に接触させても（湿式紡糸）よい。In coagulation, as shown in FIG. 1, even if the shaping polymer solution is allowed to pass through the vaporized gas portion of the coagulation liquid before it comes into contact with the coagulation liquid (dry-wet spinning), immediately after shaping as shown in FIG. It may be brought into contact with the coagulating liquid (wet spinning).
図３に示す装置は乾湿式紡糸でポリマー溶液が凝固液
と最初に接触する部分を囲い１で囲った本発明の装置の
好ましい変形を示す。囲い１により凝固液が高凝固価の
第一の凝固液と低凝固価で実質上水からなる第二の凝固
液に分割されていることは図１、図２と同じであるが、
整形高分子溶液を通過させる凝固部の囲い１の上部には
抜き取り部４が、下部には液補充部６が設けられてい
る。更に液抜き取りによる液流の乱れ防止部５、液補充
による液流の乱れ防止部７が設けられている。この様に
囲い１の両端に凝固液の出入口を設けることにより、ポ
リマー溶液と芯液から移行してくる溶剤、添加剤、非溶
剤以外の液体を液補充部６又は液抜き取り部４から注入
し、液抜き取り部４又は液補充部６から抜き取ることに
よって囲い１内部の凝固液組成を制御することも可能で
ある。The device shown in FIG. 3 shows a preferred variant of the device of the invention in which the part of the dry-wet spinning where the polymer solution first comes into contact with the coagulating liquid is surrounded by an enclosure 1. Although the coagulation liquid is divided into the first coagulation liquid having a high coagulation value and the second coagulation liquid having a low coagulation value and substantially consisting of water by the enclosure 1, as in FIGS. 1 and 2,
An extraction part 4 is provided on the upper part of the enclosure 1 of the coagulation part through which the shaping polymer solution is passed, and a liquid replenishing part 6 is provided on the lower part. Further, a liquid flow turbulence prevention unit 5 due to liquid removal and a liquid flow turbulence prevention unit 7 due to liquid replenishment are provided. In this way, by providing inlets and outlets for the coagulating liquid at both ends of the enclosure 1, liquids other than the solvent, the additive and the non-solvent, which are transferred from the polymer solution and the core liquid, are injected from the liquid replenishing unit 6 or the liquid extracting unit 4. It is also possible to control the composition of the coagulating liquid inside the enclosure 1 by extracting it from the liquid extracting unit 4 or the liquid replenishing unit 6.
以下に実施例により本発明を説明するが、本発明はこ
れらの実施例に限定されるものではない。The present invention will be described below with reference to examples, but the present invention is not limited to these examples.
比較例１ ポリエーテルサルホン20wt％、ジメチルスルホキシド
60wt％、テトラエチレンオキシド20wt％からなるポリマ
ー溶液を内径0.35mm、外径1.00mmの環状ノズルから空気
中を経て、水中に押し出して乾湿式紡糸で中空糸膜を形
成した。このノズルの中心に設けた直径0.17mmのオリフ
ィスから、中空部に押し出す芯液はジメチルスルホキシ
ド60wt％、テトラエチレンオキシド20wt％の水溶液を用
いた。得られた膜は外表面に分離機能を有し、純水透過
速度60/m2・hr・atm、ミオグロビン排除率86％であっ
た。Comparative Example 1 Polyethersulfone 20 wt%, dimethyl sulfoxide
A polymer solution consisting of 60 wt% and tetraethylene oxide 20 wt% was extruded into water through an annular nozzle having an inner diameter of 0.35 mm and an outer diameter of 1.00 mm into water to form a hollow fiber membrane by dry-wet spinning. As the core liquid extruded into the hollow portion from an orifice having a diameter of 0.17 mm provided at the center of this nozzle, an aqueous solution of 60 wt% dimethyl sulfoxide and 20 wt% tetraethylene oxide was used. The obtained membrane had a separating function on the outer surface, the pure water permeation rate was 60 / m 2 · hr · atm, and the myoglobin rejection rate was 86%.
実施例１ 中空糸状に押出されたポリマー溶液が水中に入る部分
を内径20mm、長さ300mmの筒で囲って、その他は比較例
と同じ条件で紡糸して得た膜は純水透過速度120m3/m2・
hr・atm、ミオグロビン透過率76％であった。Example 1 a hollow fiber into extruded portion inner diameter 20mm polymer solution enters the water enclosed in the cylinder of length 300 mm, others film obtained by spinning under the same conditions as comparative example pure water permeation rate 120 m 3 / m 2
The hr · atm and myoglobin transmittance were 76%.
図１、図２、図３はそれぞれ本発明の製膜装置の一例を
示す略示図、図４は従来の製膜装置の略示図である。 １……囲い、２……囲いの開口部 ３……ノズル、４……凝固液抜き取り部 5,7……液流の乱れの防止部 ６……凝固液補充部1, 2 and 3 are schematic views showing an example of the film forming apparatus of the present invention, and FIG. 4 is a schematic view of a conventional film forming apparatus. 1 ... Enclosure 2 ... Enclosure opening 3 ... Nozzle 4 ... Coagulation liquid extraction unit 5,7 ... Liquid flow turbulence prevention unit 6 ... Coagulation liquid replenishment unit
Claims (3)
からなる凝固液を充填する凝固槽を有し、凝固槽内の凝
固部に整形した高分子溶液の流れに沿う様にある距離を
隔てて囲いが設けられ、囲いの内外の非溶媒からなる凝
固液の凝固価がそれぞれ異なっている相変換法による膜
製造装置に於いて、凝固部の囲いの上部又は下部のいず
れか一方に凝固液の抜き取り部が設けられていることを
特徴とする膜製造装置。1. A nozzle section for shaping a polymer solution and a coagulation tank filled with a coagulating liquid composed of a non-solvent, and a certain distance is provided along the flow of the shaped polymer solution in the coagulation section in the coagulation tank. In a membrane manufacturing device by the phase conversion method, in which the coagulation liquids of the non-solvents inside and outside the enclosure are provided with separate enclosures and the coagulation values are different from each other, the coagulation is either on the upper part or the lower part of the enclosure of the coagulation part. A film manufacturing apparatus, characterized in that a liquid extracting portion is provided.
が設けられていることを特徴とする請求項１記載の膜製
造装置。2. The film manufacturing apparatus according to claim 1, wherein the coagulating liquid withdrawing portion is provided with a portion for preventing disturbance of the liquid flow.
の防止部を有する凝固液補充部が設けられている請求項
２記載の膜製造装置。3. The film manufacturing apparatus according to claim 2, further comprising a coagulating liquid replenishing unit having a preventing unit for disturbing the liquid flow, corresponding to the coagulating liquid extracting unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63167159A JP2527465B2 (en) | 1988-07-05 | 1988-07-05 | Membrane production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63167159A JP2527465B2 (en) | 1988-07-05 | 1988-07-05 | Membrane production equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0217926A JPH0217926A (en) | 1990-01-22 |
| JP2527465B2 true JP2527465B2 (en) | 1996-08-21 |
Family
ID=15844516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63167159A Expired - Fee Related JP2527465B2 (en) | 1988-07-05 | 1988-07-05 | Membrane production equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2527465B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPWO2020090494A1 (en) * | 2018-10-30 | 2021-09-24 | 東レ株式会社 | Hollow Fiber Membrane Spinning Cap and Hollow Fiber Membrane Manufacturing Method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5040338U (en) * | 1973-08-10 | 1975-04-24 | ||
| JPS5085320U (en) * | 1973-12-10 | 1975-07-21 | ||
| JPS53103348U (en) * | 1977-01-25 | 1978-08-19 |
-
1988
- 1988-07-05 JP JP63167159A patent/JP2527465B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0217926A (en) | 1990-01-22 |
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