JP3091015B2 - Membrane separation device - Google Patents
Membrane separation deviceInfo
- Publication number
- JP3091015B2 JP3091015B2 JP04112227A JP11222792A JP3091015B2 JP 3091015 B2 JP3091015 B2 JP 3091015B2 JP 04112227 A JP04112227 A JP 04112227A JP 11222792 A JP11222792 A JP 11222792A JP 3091015 B2 JP3091015 B2 JP 3091015B2
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fiber membrane
- raw water
- air
- outer cylinder
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Description
【０００１】[0001]
【産業上の利用分野】本発明は中空糸膜モジュ−ルを使
用した膜分離装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a membrane separation apparatus using a hollow fiber membrane module.
【０００２】[0002]
【従来の技術】近来、純水や用水の造水プロセス、食
品，製薬等の製造プロセス、排水処理プロセス等におい
て、原水から固形物質等を分離するのに膜モジュ−ルを
使用することが多い。膜モジュ−ル中、中空糸膜（外径
１ｍｍ前後）を用いた膜モジュ−ルにおいては、単位容
積当りの膜面積を大きくできるのでモジュ−ルをコンパ
クト化できる、縦型設置とすることにより、単位設置ス
ペ−ス当りの処理能力を大きくできる、等多くの利点を
有する。2. Description of the Related Art In recent years, a membrane module is often used to separate solid substances and the like from raw water in a process for producing pure water or fresh water, a process for producing food and pharmaceuticals, a process for treating waste water, and the like. . In the case of a membrane module using a hollow fiber membrane (outside diameter of about 1 mm), the membrane area per unit volume can be increased, so that the module can be made compact. It has many advantages, such as the ability to increase the processing capacity per unit installation space.
【０００３】この中空糸膜モジュ−ル中、外圧型中空糸
膜モジュ−ルにおいては、内圧型に較べ懸濁物質成分を
含む原水に対する流路詰まりが生じ難く、有利である。
勿論、濾過膜である以上、経時的な膜汚染による濾過速
度の低下が避けられず、外圧型中空糸膜モジュ−ルにお
いても、適時、膜洗浄を行う必要がある。[0003] Among the hollow fiber membrane modules, the external pressure type hollow fiber membrane module is advantageous in that the flow path of the raw water containing the suspended substance component is less likely to be clogged than the internal pressure type hollow fiber membrane module.
Of course, since it is a filtration membrane, it is inevitable that the filtration rate decreases due to membrane contamination over time, and the external pressure type hollow fiber membrane module also needs to be subjected to timely membrane cleaning.
【０００４】従来、縦型設置で使用する外圧型中空糸膜
モジュ−ルの洗浄方法として、モジュ−ルの外筒内に下
方より上方に向けエアを送入し、この送入エアによって
膜表面の付着スケ−ルをエアスクラビングする方法が公
知である。Conventionally, as a method of cleaning an external pressure type hollow fiber membrane module used in a vertical installation, air is fed upward from below into the outer cylinder of the module, and the fed air causes the surface of the membrane to be cleaned. A method of air scrubbing the scale of adhesion is known.
【０００５】このエアスクラビングによる膜洗浄法にお
いては、膜の動揺により付着スケ−ルと原水との間に剪
断力が発生し、この剪断力により付着スケ−ルの剥離が
促されることも洗浄作用に大きく寄与しており、中空糸
膜を積極的に揺動させることが有効である。このため、
従来、縦型中空糸膜モジュ−ルにおいて、中空糸膜束の
上端側のみを支持し、当該中空糸膜束の下端を自由状態
とすることが知られている。[0005] In the membrane cleaning method by air scrubbing, a shearing force is generated between the adhered scale and the raw water due to the movement of the membrane, and the peeling of the adhered scale is promoted by the shearing force. It is effective to positively swing the hollow fiber membrane. For this reason,
Conventionally, it has been known that in a vertical hollow fiber membrane module, only the upper end side of a hollow fiber membrane bundle is supported, and the lower end of the hollow fiber membrane bundle is in a free state.
【０００６】[0006]
【発明が解決しようとする課題】上記エアスクラビング
法による膜洗浄においては、送入エア圧を脈動させるこ
とが有効である。しかしながら、中空糸膜束の上端側の
みを支持し、当該中空糸膜束の下端を自由状態とした縦
型中空糸膜モジュ−ルにおいては、送入エア圧を脈動さ
せると、中空糸膜の下端部が間歇的に舞い上がりにより
曲げ変形し中空糸膜端部同士が絡み合い、網目状となり
スケ−ルが捕捉，蓄積され易く、また、中空糸膜束の下
端部が結束されてしまい、中空糸膜の揺動性が低下して
洗浄効率の低下が避けられない。In the film cleaning by the air scrubbing method, it is effective to pulsate the air pressure to be supplied. However, in a vertical hollow fiber membrane module in which only the upper end side of the hollow fiber membrane bundle is supported and the lower end of the hollow fiber membrane bundle is in a free state, when the supply air pressure is pulsated, the hollow fiber membrane The lower end portion intermittently bends and deforms due to soaring, and the ends of the hollow fiber membranes become entangled with each other to form a mesh, so that the scale is easily captured and accumulated. The oscillating property of the film is reduced, and a reduction in cleaning efficiency is inevitable.
【０００７】本発明の目的は、中空糸膜の一端を自由状
態としても、膜のエアスクラビング中、その自由端の絡
み合いを防止し得、中空糸膜の動揺性をよく保持してエ
アスクラビングによる膜洗浄を効率よく行うことのでき
る膜分離装置を提供することにある。[0007] An object of the present invention is to prevent the entanglement of the free end of the hollow fiber membrane during air scrubbing even when one end of the hollow fiber membrane is in a free state. An object of the present invention is to provide a membrane separation device capable of efficiently performing membrane cleaning.
【０００８】[0008]
【課題を解決するための手段】本発明に係る膜分離装置
は、一端を閉塞した中空糸膜の束を当該一端を上端側に
して縦型外筒内に収容し、該中空糸膜束の下端部と前記
外筒の内面との間に樹脂隔壁を形成し、前記中空糸膜束
の上端を自由端とし、樹脂隔壁下面の中空糸膜下端の開
口からの透過水を集水して取り出すための透過水室及び
透過水室の直下に存し該透過水室を経て前記樹脂隔壁に
至る原水流通用管部によって前記外筒内に連通された原
水供給口付き原水室を有するヘッダを前記の外筒下端に
設け、しかも、前記原水供給口をエアスクラビング洗浄
時のエア供給口としたことを特徴とする構成である。According to the present invention, there is provided a membrane separation apparatus comprising: a bundle of hollow fiber membranes having one end closed;
And housed in a vertical outer cylinder, the lower end of the hollow fiber membrane bundle and the
A resin partition is formed between the hollow fiber membrane bundle and the inner surface of the outer cylinder.
Open the lower end of the hollow fiber membrane on the lower surface of the resin partition
A permeated water chamber for collecting and extracting permeated water from the mouth;
It is located directly below the permeate chamber and passes through the permeate chamber to the resin partition.
The raw water communicated in the outer cylinder by the raw water distribution pipe
A header having a raw water chamber with a water supply port is provided at the lower end of the outer cylinder.
Air scrubbing cleaning of the raw water supply port
The air supply port at the time is used.
【０００９】[0009]
【作用】中空糸膜束が下端側で支持され、上端側で自由
状態であるから、下側から上側への流体流れによって
は、力学的に中空糸膜に曲げモ−メントが作用し難く、
中空糸膜同士の絡み合いをよく防止できる。従って、ス
ケ−ルを捕捉・蓄積し易い網目の発生を排除でき、ま
た、中空糸膜の揺動性をよく保持でき、エアスクラビン
グによる膜洗浄を効率よく行うことができる。Since the hollow fiber membrane bundle is supported at the lower end and is free at the upper end, bending moment does not easily act mechanically on the hollow fiber membrane depending on the fluid flow from the lower side to the upper side.
Entanglement between hollow fiber membranes can be prevented well. Therefore, it is possible to eliminate the generation of a mesh that easily captures and accumulates the scale, to maintain the oscillating property of the hollow fiber membrane, and to efficiently perform membrane cleaning by air scrubbing.
【００１０】[0010]
【実施例】以下、図面により本発明の実施例を説明す
る。図１は本発明において使用する中空糸膜モジュ−ル
Ｍを示している。図１において、１は縦型外筒である。
２は外筒内に収容した中空糸膜束である。３は外筒１の
下端に樹脂の注入によって設けた樹脂隔壁であり、中空
糸膜の下端部を支持し、中空糸膜２の下端２１を樹脂隔
壁３の外面側に開通している。中空糸膜２の上端２２は
閉塞して自由状態としてある。４は樹脂隔壁３に当間隔
を隔てて設けた複数箇の原水供給孔である。５はヘッダ
−であり、隔壁５１により原水室ａと透過水室ｂとに仕
切り、その隔壁５１に原水流通用管５２を水密に貫設
し、原水室ａには原水供給口５３を、透過水室ｂには透
過水取出口５４をそれぞれ設けてある。このヘッダ−５
を外筒１の下端にＶバンド等により連結し、原水流通用
管５２を樹脂隔壁３の原水供給孔４にＯリング等を介し
て水密に挿入してある。６は外筒１の上端に設けた原水
流出口である。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 shows a hollow fiber membrane module M used in the present invention. In FIG. 1, reference numeral 1 denotes a vertical outer cylinder.
Reference numeral 2 denotes a hollow fiber membrane bundle housed in the outer cylinder. Reference numeral 3 denotes a resin partition provided at the lower end of the outer cylinder 1 by injecting a resin, which supports the lower end of the hollow fiber membrane and opens the lower end 21 of the hollow fiber membrane 2 to the outer surface side of the resin partition 3. The upper end 22 of the hollow fiber membrane 2 is closed and in a free state. Reference numeral 4 denotes a plurality of raw water supply holes provided on the resin partition 3 at regular intervals. Reference numeral 5 denotes a header, which is partitioned by a partition wall 51 into a raw water chamber a and a permeated water chamber b, and a raw water distribution pipe 52 is provided through the partition wall 51 in a watertight manner. The permeated water outlet 54 is provided in each of the water chambers b. This header-5
Is connected to the lower end of the outer cylinder 1 by a V band or the like, and the raw water distribution pipe 52 is inserted into the raw water supply hole 4 of the resin partition wall 3 through an O-ring or the like in a watertight manner. Reference numeral 6 denotes a raw water outlet provided at the upper end of the outer cylinder 1.
【００１１】この外圧型中空糸膜モジュ−ルＭにおいて
は、原水がヘッダ−５の原水供給口５３，原水流通用管
５２並びに原水供給孔４を経て外筒１内に供給され、こ
の供給原水が上側に向かって流動していき、この間、原
水が中空糸膜２によって濾過され、この濾過により中空
糸膜内に生成した透過水がヘッダ−５の透過水室ｂを経
て透過水取出口５４から取り出されていく。他方、上記
濾過により濃縮された原水が外筒上端の原水流出口６か
ら流出していく。In the external pressure type hollow fiber membrane module M, raw water is supplied into the outer cylinder 1 through the raw water supply port 53 of the header 5, the raw water distribution pipe 52 and the raw water supply hole 4, and the raw water is supplied. Flow upward, during this time, the raw water is filtered by the hollow fiber membrane 2, and the permeated water generated in the hollow fiber membrane by this filtration passes through the permeated water chamber b of the header 5, and the permeated water outlet 54 It is taken out from. On the other hand, the raw water concentrated by the filtration flows out from the raw water outlet 6 at the upper end of the outer cylinder.
【００１２】上記縦型中空糸膜モジュ−ルにおいては、
外筒内がドレン状態となっても垂直状態の中空糸膜は自
立性を保持している。この自立性の確保のために、膜材
料として剛性の高い材質を使用したり、中空糸膜の外径
を大とし、かつ肉厚を大きくすることが有効である。前
者の高剛性膜材料としては、ポリスルホン系、ポリビニ
ルアルコ−ル系、ポリエ−テルスルホン系、ポリアクリ
ルニトリル系等を使用できる。後者の場合、中空糸膜の
充填率（中空糸膜の総断面積／外筒内断面積）２０％以
上とし（これ以下では、中空糸膜に片寄りが生じ易
い）、中空糸膜の外径を０．５ｍｍ以上とすることが好
ましい。In the above vertical hollow fiber membrane module,
Even when the inside of the outer cylinder is in the drain state, the hollow fiber membrane in the vertical state maintains autonomy. In order to secure this autonomy, it is effective to use a material having high rigidity as the membrane material, or to increase the outer diameter and the wall thickness of the hollow fiber membrane. As the former high-rigidity film material, a polysulfone-based, polyvinyl alcohol-based, polyethersulfone-based, or polyacrylonitrile-based material can be used. In the latter case, the filling rate of the hollow fiber membrane (total cross-sectional area of the hollow fiber membrane / cross-sectional area in the outer cylinder) is set to 20% or more (below this, the hollow fiber membrane tends to be deviated). Preferably, the diameter is 0.5 mm or more.
【００１３】図２は本発明の一実施例を示し、クロスフ
ロ−方式である。図２において、Ｍは上記した縦型の中
空糸膜モジュ−ルであり、並列に配設してある。７１は
原水供給ポンプ、７２は原水供給配管であり、各モジュ
−ルＭの原水供給口５３に連通してある。７３は各モジ
ュ−ルＭに対する原水供給バルブである。７４は濃縮原
水排出配管であり、管モジュ−ルＭの原水流出口６に連
通してある。７５は原水循環用配管である。７６はエア
送入配管であり、エア送入用バルブ７７を介して各モジ
ュ−ルＭの原水供給口５３に連通してある。７８はエア
排出配管である。７９は透過水配管である。８０はエア
リフト循環用配管である。この膜分離装置においては、
濃縮原水の一部を循環用配管７５によってモジュ−ルに
還流するクロスフロ−方式で濾過を行っている。FIG. 2 shows an embodiment of the present invention, which is a cross-flow system. In FIG. 2, M is the above-mentioned vertical hollow fiber membrane module, which is arranged in parallel. A raw water supply pump 71 and a raw water supply pipe 72 communicate with the raw water supply port 53 of each module M. 73 is a raw water supply valve for each module M. Reference numeral 74 denotes a concentrated raw water discharge pipe, which communicates with the raw water outlet 6 of the pipe module M. 75 is a raw water circulation pipe. Reference numeral 76 denotes an air supply pipe, which communicates with the raw water supply port 53 of each module M via an air supply valve 77. Reference numeral 78 denotes an air discharge pipe. 79 is a permeated water pipe. Reference numeral 80 denotes an air lift circulation pipe. In this membrane separation device,
Filtration is performed by a cross-flow system in which a part of the concentrated raw water is returned to the module by a circulation pipe 75.
【００１４】膜の目詰まりが進んで透過水流速が低下す
ると、原水供給ポンプ７１を停止し、原水供給バルブ７
３を閉じ、エア送入用バルブ７７を開き、各モジュ−ル
Ｍの下端に存在する原水供給口５３よりエアを各モジュ
−ルＭの外筒内に送入し、中空糸膜をエアスクラビング
により洗浄し、モジュ−ルＭの原水流出口６から流出し
ていくエアを排出配管７８より排出する。この洗浄と同
時に、または交互に、逆洗を行うこともできる（透過水
貯槽内の透過水を中空糸膜内に逆洗用ポンプまたはガス
圧により送入する）。なお、エアリフト循環用配管を利
用すると、エアリフトポンプ効果により、エアスクラビ
ング時、モジュ−ル並びに配管内で濃縮原水の循環流が
生じるため、一層の洗浄効果の向上が期待できる。When the flow rate of the permeated water decreases due to clogging of the membrane, the raw water supply pump 71 is stopped, and the raw water supply valve 7 is stopped.
3 is closed, the air inlet valve 77 is opened, and air is fed into the outer cylinder of each module M from the raw water supply port 53 present at the lower end of each module M to air scrub the hollow fiber membrane. Then, the air flowing out of the raw water outlet 6 of the module M is discharged from the discharge pipe 78. Backwashing can be performed simultaneously or alternately with this washing (permeate in the permeate storage tank is fed into the hollow fiber membrane by a backwash pump or gas pressure). If the air lift circulation pipe is used, the concentrated raw water circulates in the module and the pipe during the air scrubbing due to the air lift pump effect, so that a further improvement in the cleaning effect can be expected.
【００１５】図３は本発明の別実施例であり、全量濾過
方式であり、原水の水質が比較的良好な場合に使用され
る。この別実施例は、上記図２に示す実施例に対し、各
モジュ−ルＭの原水流出口６を開閉バルブ６１を介して
エア排出配管７８に接続した以外、図２に示す実施例と
ほぼ同一構成であり、濾過時においては、バルブ６１を
閉じて、全量濾過で原水を濾過し、エアスクラビングに
よる膜洗浄時には、バルブ６１を開いてエアを排出配管
７８から排出する。FIG. 3 shows another embodiment of the present invention, which is a total filtration system and is used when the quality of raw water is relatively good. This embodiment is substantially the same as the embodiment shown in FIG. 2 except that the raw water outlet 6 of each module M is connected to an air discharge pipe 78 via an opening / closing valve 61. The valve 61 is closed during filtration, the raw water is filtered by total filtration, and the valve 61 is opened to discharge air from the discharge pipe 78 during membrane cleaning by air scrubbing.
【００１６】上記において、原水供給ポンプの停止，再
駆動、洗浄の開始，停止，再開，洗浄の切り替え（エア
スクラビングによる膜洗浄と逆洗との切り替え）等は通
常自動操作によって行われる。In the above description, the stop and restart of the raw water supply pump, the start, stop and restart of washing, and the switching of washing (switching between membrane washing and back washing by air scrubbing) are usually performed automatically.
【００１７】本発明の膜分離装置においては、中空糸膜
を片端支持、他端自由状態の縦型中空糸膜モジュ−ルを
使用しているが、膜洗浄時の下側からのエアの送入に対
し、その中空糸膜の自由端を上側に存在させてあるか
ら、中空糸膜の自由端の舞い上がりによる絡み合いを排
除でき、中空糸膜の揺動性をよく保持でき、エアスクラ
ビングによる膜洗浄を効率よく行うことができる。この
ことは、次ぎの実施例と比較例との試験結果からも確認
できる。In the membrane separation apparatus of the present invention, the hollow fiber membrane is supported at one end and the vertical hollow fiber membrane module in which the other end is free is used. Since the free end of the hollow fiber membrane is present on the upper side, the entanglement due to the rising of the free end of the hollow fiber membrane can be eliminated, the swingability of the hollow fiber membrane can be maintained well, and the membrane by air scrubbing can be maintained. Cleaning can be performed efficiently. This can be confirmed also from the test results of the following examples and comparative examples.
【００１８】実施例 モジュ−ルには、図１に示す中空糸膜の上端が自由状態
の縦型中空糸膜モジュ−ルであって、内径１２５ｍｍ
φ，長さ１０７７ｍｍの外筒内に、外径２．０ｍｍ，内
径１．２ｍｍ，平均孔径０．１μｍの多孔ポリスルホン
製中空糸膜を１０００本充填したもの（総膜面積５
ｍ2）を１台使用し、河川水（濁度１〜１０度）を前処
理なしで定圧全量濾過にて、エアスクラビングよる膜洗
浄を一回／日，逆洗洗浄を一回／１時間の頻度で行いつ
つ６ヵ月間にわたり濾過をつづけた。この間の初期透過
水量に対する保持率を測定したところ図４のイの通りで
あった。EXAMPLE The module is a vertical hollow fiber membrane module in which the upper end of the hollow fiber membrane shown in FIG. 1 is in a free state and has an inner diameter of 125 mm.
An outer cylinder of φ, 1077 mm in length filled with 1,000 hollow fiber membranes made of porous polysulfone having an outer diameter of 2.0 mm, an inner diameter of 1.2 mm, and an average pore diameter of 0.1 μm (total membrane area of 5
m 2 ), river water (turbidity 1 to 10 degrees) is subjected to constant pressure and total volume filtration without pretreatment, and membrane cleaning by air scrubbing is performed once a day and backwashing is performed once a hour. The filtration was continued over a period of 6 months while performing the above. The retention rate of the initial permeated water amount during this time was measured and was as shown in FIG.
【００１９】比較例 中空糸膜の下端を自由状態とし、原水供給口を外筒の上
端に設けた以外は実施例と同様にして（図１に示す縦型
中空糸膜モジュ−ルを上下逆にして設置し、原水流出口
からエアスクラビング用のエアを送入した）、初期透過
水量に対する保持率を測定したところ図４のロの通りで
あった。Comparative Example A vertical hollow fiber membrane module shown in FIG. 1 was turned upside down except that the lower end of the hollow fiber membrane was in a free state and the raw water supply port was provided at the upper end of the outer cylinder. , And the air for air scrubbing was fed in from the raw water outlet), and the retention rate with respect to the initial permeated water amount was measured.
【００２０】この試験結果からも明らかなように、本発
明の膜分離装置は洗浄効率に優れており、比較例では中
空糸膜の自由端の絡み合いが観られたが、実施例におい
てはもとのままであった。As is clear from the test results, the membrane separation device of the present invention is excellent in cleaning efficiency, and the entanglement of the free end of the hollow fiber membrane was observed in the comparative example. It was still.
【００２１】[0021]
【発明の効果】本発明の膜分離装置においては、通常の
外圧型の中空糸膜束吊り下げ式のモジュ−ルを上下逆に
して設置し、ヘッダの原水供給口をエアスクラビング洗
浄時のエア供給口とした構成であり、エアノズル等の特
別のエア供給手段を設けることなく簡易・小型のモジュ
−ルのもとで高効率のエアスクラビング洗浄を保証でき
る。According to the membrane separation apparatus of the present invention, the usual
External pressure type hollow fiber membrane bundle hanging type module upside down
And clean the header water supply port with air scrubbing.
It is configured as an air supply port at the time of cleaning.
Simple and compact module without separate air supply means
-Ensure high efficiency air scrubbing cleaning
You .
【図１】本発明において使用する縦型中空糸膜モジュ−
ルを示す断面説明図である。FIG. 1 is a vertical hollow fiber membrane module used in the present invention.
FIG.
【図２】本発明の実施例を示す説明図である。FIG. 2 is an explanatory diagram showing an embodiment of the present invention.
【図３】本発明の別実施例を示す説明図である。FIG. 3 is an explanatory view showing another embodiment of the present invention.
【図４】本発明の膜分離装置と従来例との濾過性能を示
す図表である。FIG. 4 is a table showing the filtration performance of the membrane separation device of the present invention and a conventional example.
１ 外筒 ２ 中空糸膜 ２１ 中空糸膜の下端 ２２ 中空糸膜の上端 ５３ 原水供給口 ７６ エア送入配管 Reference Signs List 1 outer cylinder 2 hollow fiber membrane 21 lower end of hollow fiber membrane 22 upper end of hollow fiber membrane 53 raw water supply port 76 air supply pipe
───────────────────────────────────────────────────── フロントページの続き (72)発明者 田原 伸治 大阪府茨木市下穂積１丁目１番２号 日 東電工株式会社内 (56)参考文献 特開 昭62−155906（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 63/02 B01D 65/02 520 ──────────────────────────────────────────────────続 き Continuation of front page (72) Inventor Shinji Tahara 1-2-1 Shimohozumi, Ibaraki-shi, Osaka Nippon Denko Corporation (56) References JP-A-62-155906 (JP, A) (58) ) Surveyed field (Int. Cl. 7 , DB name) B01D 63/02 B01D 65/02 520
Claims (1)
上端側にして縦型外筒内に収容し、該中空糸膜束の下端
部と前記外筒の内面との間に樹脂隔壁を形成し、前記中
空糸膜束の上端を自由端とし、樹脂隔壁下面の中空糸膜
下端の開口からの透過水を集水して取り出すための透過
水室及び透過水室の直下に存し該透過水室を経て前記樹
脂隔壁に至る原水流通用管部によって前記外筒内に連通
された原水供給口付き原水室を有するヘッダを前記の外
筒下端に設け、しかも、前記原水供給口をエアスクラビ
ング洗浄時のエア供給口としたことを特徴とする膜分離
装置。1. A bundle of hollow fiber membranes having one end closed,
The upper end is housed in a vertical outer cylinder, and the lower end of the hollow fiber membrane bundle
Forming a resin partition between the portion and the inner surface of the outer cylinder;
The hollow fiber membrane on the lower surface of the resin partition is the free end at the upper end of the empty fiber membrane bundle.
Permeation for collecting and extracting permeated water from the lower opening
A water chamber and a permeated water chamber.
The inside of the outer cylinder is communicated with the raw water distribution pipe to the oil partition
The header having the raw water chamber with the raw water supply port
At the lower end of the cylinder, and connect the raw water supply port with an air scrub
A membrane separation device characterized by an air supply port for cleaning .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04112227A JP3091015B2 (en) | 1992-04-03 | 1992-04-03 | Membrane separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04112227A JP3091015B2 (en) | 1992-04-03 | 1992-04-03 | Membrane separation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05285349A JPH05285349A (en) | 1993-11-02 |
| JP3091015B2 true JP3091015B2 (en) | 2000-09-25 |
Family
ID=14581438
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP04112227A Expired - Fee Related JP3091015B2 (en) | 1992-04-03 | 1992-04-03 | Membrane separation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3091015B2 (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5639373A (en) | 1995-08-11 | 1997-06-17 | Zenon Environmental Inc. | Vertical skein of hollow fiber membranes and method of maintaining clean fiber surfaces while filtering a substrate to withdraw a permeate |
| DE69636130T2 (en) | 1995-08-11 | 2006-12-07 | Zenon Environmental Inc., Oakville | Permeatsammelsystem |
| US7087173B2 (en) | 1995-08-11 | 2006-08-08 | Zenon Environmental Inc. | Inverted cavity aerator for membrane module |
| US6685832B2 (en) | 1995-08-11 | 2004-02-03 | Zenon Environmental Inc. | Method of potting hollow fiber membranes |
| US8852438B2 (en) | 1995-08-11 | 2014-10-07 | Zenon Technology Partnership | Membrane filtration module with adjustable header spacing |
| DE10045227C1 (en) * | 2000-09-13 | 2002-02-07 | Vosenkaul Klaus | Membrane filter for water treatment uses capillary membrane fibre bundle projecting into untreated water and fitting into permeate collection space at opposite end |
| JP2003094058A (en) * | 2001-09-27 | 2003-04-02 | Daicel Chem Ind Ltd | Method for treating water |
| DE10161095C1 (en) * | 2001-12-12 | 2002-11-07 | Klaus Vosenkaul | Process for membrane filtration of liquids e.g. water, uses fiber bundle of capillary membranes having one end cast in headpiece open to permeate collecting chamber of the headpiece and a freely moving closed end |
| KR100569681B1 (en) | 2003-11-17 | 2006-04-10 | 주식회사 코오롱 | Submerged hollow fiber membrane module |
| FR2867394B1 (en) * | 2004-03-10 | 2006-12-15 | Degremont | METHOD OF CLEANING FILTRATION MEMBRANES, AND INSTALLATION FOR CARRYING OUT SAID METHOD |
| WO2011065418A1 (en) * | 2009-11-26 | 2011-06-03 | 株式会社神鋼環境ソリューション | Hollow-fiber membrane module, water treatment device, membrane separation method, and water treatment method |
| JP2011110499A (en) * | 2009-11-26 | 2011-06-09 | Kobelco Eco-Solutions Co Ltd | Hollow fiber membrane module and water treatment method |
| JP2011110496A (en) * | 2009-11-26 | 2011-06-09 | Kobelco Eco-Solutions Co Ltd | Hollow fiber membrane module, membrane separation method, and water treatment apparatus |
| JP2011110498A (en) * | 2009-11-26 | 2011-06-09 | Kobelco Eco-Solutions Co Ltd | Hollow fiber membrane module and water treatment method |
| JP6322882B2 (en) * | 2012-03-30 | 2018-05-16 | 栗田工業株式会社 | Pretreatment device for online measurement in water system, online measurement device using the pretreatment device for online measurement, pretreatment method in online measurement, and online measurement method using the pretreatment method |
| JP2015188769A (en) * | 2014-03-27 | 2015-11-02 | 栗田工業株式会社 | Pretreatment apparatus for online measurement in aqueous system, online measuring apparatus including the same, and pretreatment method for online measurement |
| CN107224878B (en) * | 2017-08-04 | 2023-05-30 | 金科环境股份有限公司 | Universal valve group for ultrafiltration device |
-
1992
- 1992-04-03 JP JP04112227A patent/JP3091015B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH05285349A (en) | 1993-11-02 |
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