JP2006082001A - Membrane separator - Google Patents
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Abstract
【課題】 長期間安定した濾過を可能とする膜分離装置の提供。
【解決手段】 多数本の中空糸膜からなる中空糸膜束の、両端部が接着固定され、上端部に中空糸膜の開口部を有し、下端部に気体導入用のスカート構造部と気体を中空糸膜外表面に導入する気体導入孔を有し、かつ垂直方向に設置される膜モジュールと、該スカート構造部の下部に噴出部を有する散気装置とから構成される膜分離装置であって、該散気装置が、集水管と平行に設置されかつ給気手段に連通する散気装置用主パイプ、主パイプに対して鉛直方向に分岐された散気装置用分枝パイプ、さらに、分岐パイプの末端部に取り付けられた噴出口を２つ以上有する噴出部から構成されることを特徴とする膜分離装置。
【選択図】 選択図なしPROBLEM TO BE SOLVED: To provide a membrane separation device capable of stable filtration for a long period of time.
SOLUTION: A hollow fiber membrane bundle comprising a plurality of hollow fiber membranes is bonded and fixed at both ends, has a hollow fiber membrane opening at the upper end, and a skirt structure for introducing gas at the lower end and gas A membrane separation device comprising a membrane module having a gas introduction hole for introducing a gas into an outer surface of a hollow fiber membrane and installed in a vertical direction, and an air diffuser having a jet part at a lower portion of the skirt structure portion The air diffuser is installed in parallel with the water collecting pipe and communicates with the air supply means, the main pipe for the air diffuser, the branch pipe for the air diffuser branched in the vertical direction with respect to the main pipe, A membrane separation device comprising an ejection portion having two or more ejection ports attached to an end portion of a branch pipe.
[Selection figure] No selection figure
Description
本発明は、膜分離装置に関する。 The present invention relates to a membrane separation apparatus.
従来、浄水処理、下水処理、産業排水処理等における固液分離は、凝集沈殿槽、重力沈殿槽等を用いて行われていた。しかしながら、近年では、膜技術の発達により、上述した各種の槽に比べてコンパクトな槽を用い、この中に膜モジュールを浸漬させて、被処理水を固液分離する方法が採用されるに至っている。即ち、槽内に供給された懸濁物質を含む被処理水中に上述した膜モジュールを設置し、この膜モジュールにおいて加圧、吸引もしくは水頭差により濾過を行い、膜モジュールによって濾過された濾過水が槽の外部に引き出される。このような方法によれば、槽内の液相中の懸濁物質は、膜モジュールの供給側に固形分として残り、膜モジュールの透過側において、除濁、除菌された清浄な濾過水が得られる。 Conventionally, solid-liquid separation in water purification treatment, sewage treatment, industrial wastewater treatment, and the like has been performed using a coagulation sedimentation tank, a gravity sedimentation tank, and the like. However, in recent years, due to the development of membrane technology, a method has been adopted in which a compact tank is used in comparison with the various tanks described above, and the membrane module is immersed in the tank to separate the water to be treated from solid and liquid. Yes. That is, the membrane module described above is installed in the water to be treated containing suspended solids supplied into the tank, and filtration is performed by pressurization, suction, or water head difference in this membrane module, and the filtered water filtered by the membrane module is It is pulled out of the tank. According to such a method, the suspended substance in the liquid phase in the tank remains as a solid content on the supply side of the membrane module, and clean filtered water that has been turbidized and sterilized on the permeate side of the membrane module. can get.
このような膜分離装置においては、濾過を長期間安定させるため、効果的な物理洗浄が必要である。すなわち、濾過膜の二次側から一次側へ膜濾過水を逆流させる逆洗や散気装置により気体を噴出させ、気体の上昇により生じる水流によって膜面を洗浄する空洗などの物理洗浄により膜面に堆積した懸濁物質を剥離させ、かつ、剥離した懸濁物質を系外へ排出する必要がある。ここで、空洗による物理洗浄方法は、散気装置から噴出した気体を膜モジュール全体へ均一に供給しなければ効果的な洗浄効果を得ることができない。すなわち、散気装置により噴出した気体が膜モジュールに対して片流れを起こした場合、気体が流れない箇所においては十分な膜面洗浄流を得られないため、膜面に堆積した懸濁物質が剥離されず濾過能力が急激に低下していく。 In such a membrane separation device, effective physical cleaning is necessary to stabilize filtration for a long period of time. That is, the membrane is washed by physical washing such as backwashing that reverses the membrane filtrate water from the secondary side to the primary side of the filtration membrane or by jetting the gas with an air diffuser and washing the membrane surface with the water flow generated by the rising of the gas. It is necessary to exfoliate the suspended substance deposited on the surface and to discharge the exfoliated suspended substance out of the system. Here, the physical cleaning method by air washing cannot obtain an effective cleaning effect unless the gas ejected from the air diffuser is uniformly supplied to the entire membrane module. In other words, when the gas blown out by the diffuser causes a single flow to the membrane module, a sufficient membrane surface cleaning flow cannot be obtained where gas does not flow. The filtration capacity is suddenly reduced.
このような問題に鑑み、膜モジュール全体へ均一に気体を供給し、効果的な膜面洗浄流を発生させるために、散気装置の主パイプに多数の噴出口を取り付けた膜分離装置用散気装置（特許文献１）が開示されている。又、散気装置の主パイプから分岐パイプを複数本有した浸漬型膜分離装置用の散気装置（特許文献２）や、膜モジュールが設置された槽全体へ均一に気体を供給するために、槽断面積に対して気体吐出口の個数を規定した散気装置（特許文献３）、さらには、設置した膜モジュールに対して傾斜をつけて散気装置を配置した膜分離装置（特許文献４）が開発されている。
しかしながら、前述した膜分離装置では、気体を膜モジュール全体へ均一に供給することができず、気体が流れない箇所において十分な膜面洗浄流を得られないため、膜面に堆積した懸濁物質が剥離されず濾過能力が急激に低下してしまう問題を解決することはできない。
However, in the above-described membrane separation apparatus, the gas cannot be uniformly supplied to the entire membrane module, and a sufficient membrane surface cleaning flow cannot be obtained at a location where the gas does not flow. However, the problem that the filtration ability is rapidly lowered without being peeled off cannot be solved.
本発明は、長期間安定した濾過を可能とする膜分離装置を提供することを目的とする。 An object of this invention is to provide the membrane separator which enables the stable filtration for a long period of time.
本発明者らは、鋭意検討の結果、散気装置用主パイプに対して鉛直方向に延びた分岐パイプの末端部に取り付けた噴出部に噴出口を２つ以上にすることで、気体を確実に膜モジュールへ供給し、かつ、気体の片流れを防止できることを見出し、本発明を完成するに至った。 As a result of intensive studies, the present inventors have ensured gas by providing two or more jet outlets in the jet part attached to the end part of the branch pipe extending in the vertical direction with respect to the main pipe for the diffuser. The present invention has been completed by finding that it can be supplied to the membrane module and gas flow can be prevented from flowing.
すなわち、本発明は、
（１）多数本の中空糸膜からなる中空糸膜束の、両端部が接着固定され、上端部に中空糸膜の開口部を有し、下端部に気体導入用のスカート構造部と気体を中空糸膜外表面に導入する気体導入孔を有し、かつ垂直方向に設置される膜モジュールと、該スカート構造部の下部に噴出部を有する散気装置とから構成される膜分離装置であって、該散気装置が、集水管と平行に設置されかつ給気手段に連通する散気装置用主パイプ、主パイプに対して鉛直方向に分岐された散気装置用分枝パイプ、さらに、分岐パイプの末端部に取り付けられた噴出口を２つ以上有する噴出部から構成されることを特徴とする膜分離装置。
That is, the present invention
(1) Both ends of a bundle of hollow fiber membranes comprising a plurality of hollow fiber membranes are bonded and fixed, the upper end portion has an opening of the hollow fiber membrane, and the lower end portion has a gas introduction skirt structure portion and gas. A membrane separation device comprising a membrane module having a gas introduction hole to be introduced into the outer surface of a hollow fiber membrane and installed in a vertical direction, and an air diffuser having an ejection portion below the skirt structure. The air diffuser is installed in parallel with the water collecting pipe and communicates with the air supply means, the main pipe for the air diffuser, the branch pipe for the air diffuser branched in the vertical direction with respect to the main pipe, A membrane separation device comprising a jetting portion having two or more jetting ports attached to an end portion of a branch pipe.
（２）噴出部が分岐パイプを中心として対称となるよう配置された噴出口を有し、かつ、噴出口が噴出流により回転可能な状態で分岐パイプに取り付けられていることを特徴とする（１）に記載の膜分離装置。
（３）噴出部が側面に複数個のスリットを有するキャップにより形成されており、前記キャップを分岐パイプの末端部に取り付けてあることを特徴とする（１）または（２）に記載の膜分離装置。
（４）噴出部が膜モジュールの中心に対して直下にあることを特徴とする（１）〜（３）のいずれかに記載の膜分離装置。
（５）噴出部と膜モジュール下端面との距離が５〜２００ｍｍであることを特徴とする（１）〜（４）のいずれかに記載の膜分離装置、である。
(2) The jet part has a jet port arranged so as to be symmetric about the branch pipe, and the jet port is attached to the branch pipe so as to be rotatable by the jet flow ( The membrane separator according to 1).
(3) The membrane separation according to (1) or (2), wherein the ejection part is formed by a cap having a plurality of slits on a side surface, and the cap is attached to a terminal part of the branch pipe. apparatus.
(4) The membrane separation device according to any one of (1) to (3), wherein the ejection portion is directly below the center of the membrane module.
(5) The membrane separation device according to any one of (1) to (4), wherein a distance between the ejection portion and the lower end surface of the membrane module is 5 to 200 mm.
本発明の膜分離装置を用いることにより、気体が片流れを起こさず均一に膜モジュールへ供給されるので、効果的な物理洗浄を行うことが出来、よって、長期間の安定運転が可能となる。 By using the membrane separation apparatus of the present invention, gas is uniformly supplied to the membrane module without causing a single flow, so that effective physical cleaning can be performed, and thus stable operation for a long period of time is possible.
以下、本発明に関して、好ましい実施形態を中心に、詳細に説明する。
図１は、圧縮空気などの給気手段と連通した散気装置用主パイプが、複数本の膜モジュールが配置された集水管と水平方向に設置され、かつ、前記主パイプに対して鉛直方向に分岐された散気装置用分枝パイプで構成され、さらに、分岐パイプの末端部に取り付けた噴出部の形状がＴ字型（噴出口を２つ有する）である本発明の膜分離装置の一例を示す概略図である。１は圧縮空気などの給気手段、２は散気装置用主パイプ、３は散気装置用分岐パイプ、４はＴ型噴出部、５は膜モジュール気体導入孔、６は膜モジュール、７は集水管を示している。
Hereinafter, the present invention will be described in detail focusing on preferred embodiments.
FIG. 1 shows that a main pipe for an air diffuser communicated with an air supply means such as compressed air is installed in a horizontal direction with a water collecting pipe in which a plurality of membrane modules are arranged, and is perpendicular to the main pipe. The membrane separation device of the present invention is composed of a branch pipe for an air diffuser that is branched into two, and the shape of the jet part attached to the end of the branch pipe is T-shaped (having two jet ports) It is the schematic which shows an example. 1 is an air supply means such as compressed air, 2 is a main pipe for an air diffuser, 3 is a branch pipe for an air diffuser, 4 is a T-type jet part, 5 is a gas inlet for a membrane module, 6 is a membrane module, 7 is Shows the water collection pipe.
図１に示した膜分離装置を用いることにより、気体を確実に膜モジュールへ供給し、かつ、気体の片流れを防止できる。ここで、図１に示した噴出部の形状は本発明の一例であり、噴出部の噴出口が２つ以上あればどんな形状でも良いが、例えば、噴出口が分岐パイプを中心として対称となるよう配置され、かつ、噴出口からの噴出流により回転可能な状態で分岐パイプに取り付けてある場合や、側面が複数個のスリットを有するキャップにより形成されており、前記キャップを分岐パイプの末端部に取り付けてある場合等は、気体が片流れを起こさず均一に膜モジュールへ供給され、効果的な物理洗浄が可能となり好ましい。 By using the membrane separation apparatus shown in FIG. 1, it is possible to reliably supply gas to the membrane module and to prevent a single gas flow. Here, the shape of the ejection portion shown in FIG. 1 is an example of the present invention, and any shape may be used as long as the ejection portion has two or more ejection ports. For example, the ejection port is symmetric about the branch pipe. Arranged on the branch pipe in a state where it can be rotated by the jet flow from the jet outlet, or the side surface is formed by a cap having a plurality of slits, and the cap is connected to the end of the branch pipe. The gas is preferably supplied to the membrane module uniformly without causing a single flow, enabling effective physical cleaning.
また、散気装置用主パイプ及び散気装置用分岐パイプの配置箇所は一例にすぎずこれに限定されるものではない。また、噴出部は膜モジュールの中心に対して直下に配置されることが好ましく、噴出部と膜モジュール下端面との距離は５〜２００ｍｍが好ましい。
ここで、本発明に用いる膜モジュールとしては、中空糸膜の上下端部が接着固定され、どちらか一方の端部の中空糸膜が開口されたものであり、接着固定される端部の断面形状としては、円形の他、三角形、四角形、六角形、楕円形等であってもよい。また、膜モジュールに用いる中空糸膜としては、ナノ濾過膜、限外濾過膜、あるいは精密濾過膜等のいずれでもよい。さらに、接着固定された端部のどちらか一方には、気体導入用の複数の気体導入孔を有するものが好ましい。
Moreover, the arrangement | positioning location of the main pipe for diffusers and the branch pipe for diffusers is only an example, and is not limited to this. Moreover, it is preferable that an ejection part is arrange | positioned directly under the center of a membrane module, and the distance of an ejection part and a membrane module lower end surface has preferable 5-200 mm.
Here, as the membrane module used in the present invention, the upper and lower ends of the hollow fiber membrane are bonded and fixed, and the hollow fiber membrane at one of the ends is opened, and the cross section of the end to be bonded and fixed The shape may be a circle, a triangle, a quadrangle, a hexagon, an ellipse, or the like. The hollow fiber membrane used in the membrane module may be any of a nanofiltration membrane, an ultrafiltration membrane, a microfiltration membrane, or the like. Furthermore, it is preferable to have a plurality of gas introduction holes for introducing gas at either one of the bonded and fixed end portions.
本発明を実施例に基づいて説明する。
［実施例１］
散気装置用主パイプに対して鉛直方向に分岐された散気装置用分枝パイプで構成され、さらに、前記分岐パイプの末端部に取り付けた噴出部の形状がＴ字型である散気装置２を取り付けた膜分離装置を用いて、濾過、逆洗、空洗、物理洗浄排水の排出からなる運転工程にて、河川水の濾過をおこなった。空洗流量は４Ｎｍ３／ｈｒ／膜モジュールである。使用した膜モジュールは、直径１６５ｍｍ、長さ２ｍであり、ポリフッ化ビニリデン製の公称孔径０．１μｍの中空糸型精密濾過膜を膜面積５０ｍ２に束ねたものを用いた。膜濾過流束２．４ｍ3／ｍ2／日（膜面積１ｍ2で1日あたり２．４ｍ3の濾過水が得られる流束）で安定した濾過運転が可能であった。これは、Ｔ字型の噴出部を分岐パイプの先端に取り付け、前記噴出部を膜モジュールの真下に配置し、かつ、噴出部と膜モジュール下端面との距離を８０ｍｍ確保したことにより、気体が片流れを起こさず均一に膜モジュールへ供給され、効果的な物理洗浄がおこなわれたためである。
The present invention will be described based on examples.
[Example 1]
An air diffuser comprising a branch pipe for an air diffuser branched in a vertical direction with respect to the main pipe for the air diffuser, and further having a T-shaped jet part attached to the end of the branch pipe River water was filtered using a membrane separation apparatus equipped with No. 2 in the operation process consisting of filtration, backwashing, air washing, and physical washing drainage. The air washing flow rate is 4 Nm 3 / hr / membrane module. The membrane module used had a diameter of 165 mm and a length of 2 m, and a hollow fiber type microfiltration membrane made of polyvinylidene fluoride and having a nominal pore diameter of 0.1 μm was bundled in a membrane area of 50 m 2 . A stable filtration operation was possible with a membrane filtration flux of 2.4 m 3 / m 2 / day (a flux that gave 2.4 m 3 of filtered water per day with a membrane area of 1 m 2 ). This is because the T-shaped ejection part is attached to the tip of the branch pipe, the ejection part is arranged directly below the membrane module, and the distance between the ejection part and the lower end surface of the membrane module is secured to 80 mm. This is because the film was uniformly supplied to the membrane module without causing a single flow, and an effective physical cleaning was performed.
［比較例１］
噴出部の噴出口が１つの散気装置１を取り付けた膜分離装置を用いて、濾過、逆洗、空洗、物理洗浄排水の排出からなる運転工程にて、河川水の濾過をおこなった。空洗流量は４Ｎｍ３／ｈｒ／膜モジュールである。使用した膜モジュールは実施例１に記載したものを使用した。膜濾過流束２．４ｍ3／ｍ2／日で濾過圧力が上昇を続けた。これは、噴出部を膜モジュールの真下に配置し、かつ、噴出部と膜モジュール下端面との距離を８０ｍｍ確保したにも関わらず、分岐パイプに取り付けた噴出口が１つしか無かったために、気体が片流れを起こし、均一に膜モジュールへ供給されず、効果的な物理洗浄がおこなわれなかったためである。図２は、散気装置２（Ｔ型噴出部あり）との膜濾過試験結果の比較を示すグラフである。
[Comparative Example 1]
River water was filtered in the operation process consisting of filtration, backwashing, air washing, and discharge of physical washing drainage using a membrane separation apparatus having a single air diffuser 1 at the jetting part of the jetting part. The air washing flow rate is 4 Nm 3 / hr / membrane module. The membrane module used was that described in Example 1. The filtration pressure continued to increase at a membrane filtration flux of 2.4 m 3 / m 2 / day. This is because there was only one jet outlet attached to the branch pipe despite the fact that the jet part was arranged directly under the membrane module and the distance between the jet part and the membrane module lower end surface was 80 mm. This is because the gas caused a single flow, was not uniformly supplied to the membrane module, and effective physical cleaning was not performed. FIG. 2 is a graph showing a comparison of the results of the membrane filtration test with the diffuser 2 (with a T-type ejection part).
［実施例２］
散気装置用主パイプに対して鉛直方向に分岐された散気装置用分枝パイプで構成され、さらに、前記分岐パイプの末端部に取り付けた噴出口が分岐パイプを中心として対称となるよう配置され、かつ、噴出口からの噴出流により回転可能である散気装置（図３）を取り付けた膜分離装置を用いて、濾過、逆洗、空洗、物理洗浄排水の排出からなる運転工程にて、河川水の濾過をおこなった。空洗流量は４Ｎｍ３／ｈｒ／膜モジュールである。使用した膜モジュールは、直径１６５ｍｍ、長さ２ｍであり、ポリフッ化ビニリデン製の公称孔径０．１μｍの中空糸型精密濾過膜を膜面積５０ｍ２に束ねたものを用いた。膜濾過流束２．４ｍ3／ｍ2／日で安定した濾過運転が可能であった。これは、噴出口からの噴出流により回転可能な噴出部を分岐パイプの先端に取り付け、前記噴出部を膜モジュールの真下に配置し、かつ、噴出部と膜モジュール下端面との距離を８０ｍｍ確保したことにより、気体が片流れを起こさず均一に膜モジュールへ供給され、効果的な物理洗浄がおこなわれたためである。
[Example 2]
Consists of a branch pipe for the diffuser that is branched in the vertical direction with respect to the main pipe for the diffuser, and is further arranged so that the jet outlet attached to the end of the branch pipe is symmetrical about the branch pipe In addition, a membrane separation device equipped with an air diffuser (FIG. 3) that can be rotated by a jet flow from a jet outlet is used to perform an operation process including filtration, backwashing, air washing, and physical washing drainage discharge. The river water was filtered. The air washing flow rate is 4 Nm 3 / hr / membrane module. The membrane module used had a diameter of 165 mm and a length of 2 m, and a hollow fiber type microfiltration membrane made of polyvinylidene fluoride and having a nominal pore diameter of 0.1 μm was bundled in a membrane area of 50 m 2 . A stable filtration operation was possible at a membrane filtration flux of 2.4 m 3 / m 2 / day. This is because a jet part that can be rotated by the jet flow from the jet outlet is attached to the tip of the branch pipe, the jet part is arranged directly under the membrane module, and the distance between the jet part and the lower end surface of the membrane module is secured to 80 mm. This is because the gas was uniformly supplied to the membrane module without causing a single flow, and an effective physical cleaning was performed.
［実施例３］
散気装置用主パイプに対して鉛直方向に分岐された散気装置用分枝パイプで構成され、さらに、前記分岐パイプの末端部に取り付けた噴出口が側面に複数個のスリットを有する盲キャップにより形成された散気装置（図４）を取り付けた膜分離装置を用いて、濾過、逆洗、空洗、物理洗浄排水の排出からなる運転工程にて、河川水の濾過をおこなった。空洗流量は４Ｎｍ３／ｈｒ／膜モジュールである。使用した膜モジュールは、直径１６５ｍｍ、長さ２ｍであり、ポリフッ化ビニリデン製の公称孔径０．１μｍの中空糸型精密濾過膜を膜面積５０ｍ２に束ねたものを用いた。膜濾過流束２．４ｍ3／ｍ2／日で安定した濾過運転が可能であった。これは、側面に複数個のスリットを有する噴出部を分岐パイプの先端に取り付け、前記噴出部を膜モジュールの真下に配置し、かつ、噴出部と膜モジュール下端面との距離を８０ｍｍ確保したことにより、気体が片流れを起こさず均一に膜モジュールへ供給され、効果的な物理洗浄がおこなわれたためである。
[Example 3]
A blind cap comprising a branch pipe for an air diffuser branched in a vertical direction with respect to the main pipe for the air diffuser, and further having a plurality of slits on a side surface of an outlet attached to the end of the branch pipe River water was filtered in the operation process consisting of filtration, backwashing, air washing, and discharge of physical washing drainage using a membrane separation apparatus equipped with an air diffuser formed by (4). The air washing flow rate is 4 Nm 3 / hr / membrane module. The membrane module used had a diameter of 165 mm and a length of 2 m, and a hollow fiber type microfiltration membrane made of polyvinylidene fluoride and having a nominal pore diameter of 0.1 μm was bundled in a membrane area of 50 m 2 . A stable filtration operation was possible at a membrane filtration flux of 2.4 m 3 / m 2 / day. This is because a jet part having a plurality of slits on the side surface is attached to the tip of the branch pipe, the jet part is arranged directly under the membrane module, and the distance between the jet part and the lower end surface of the membrane module is 80 mm. This is because the gas was uniformly supplied to the membrane module without causing a single flow, and an effective physical cleaning was performed.
本発明は、膜分離装置に関する分野で好適に利用できる。 The present invention can be suitably used in the field related to membrane separation apparatuses.
１ 給気手段
２ 散気装置用主パイプ
３ 散気装置用分岐パイプ
４ Ｔ型噴出部
５ 膜モジュール気体導入孔
６ 膜モジュール
７ 集水管
DESCRIPTION OF SYMBOLS 1 Air supply means 2 Main pipe for
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2004268835A JP2006082001A (en) | 2004-09-15 | 2004-09-15 | Membrane separator |
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|---|---|---|---|
| JP2004268835A JP2006082001A (en) | 2004-09-15 | 2004-09-15 | Membrane separator |
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| JP2006082001A true JP2006082001A (en) | 2006-03-30 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010069361A (en) * | 2008-09-16 | 2010-04-02 | Mitsubishi Rayon Eng Co Ltd | Membrane washing apparatus, membrane separation apparatus, and wastewater treatment apparatus |
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| JPS56121422A (en) * | 1980-02-25 | 1981-09-24 | Yamakuni Tetsukou Kk | Fish preserve apparatus |
| JPS6279898A (en) * | 1985-10-03 | 1987-04-13 | Kubota Ltd | Aeration tank air diffuser |
| JPH06328093A (en) * | 1993-05-27 | 1994-11-29 | Matsushita Electric Works Ltd | Sewage treatment equipment air supply device |
| JPH09131518A (en) * | 1995-11-09 | 1997-05-20 | Hitachi Ltd | Filtration device |
| JPH1094720A (en) * | 1996-09-24 | 1998-04-14 | Kuraray Co Ltd | Hollow fiber membrane module |
| JPH1099882A (en) * | 1996-09-30 | 1998-04-21 | Kubota Corp | Diffuser |
| JP2000157099A (en) * | 1998-11-26 | 2000-06-13 | Mishio Kiko Kk | Rotary air nozzle for culture |
| WO2002004101A1 (en) * | 2000-07-10 | 2002-01-17 | Asahi Kasei Kabushiki Kaisha | Hollow thread film cartridge, hollow thread film module using the cartridge, and tank type filter |
| JP2002336663A (en) * | 2001-05-17 | 2002-11-26 | Japan Organo Co Ltd | Filtration apparatus |
| JP2004008981A (en) * | 2002-06-10 | 2004-01-15 | Asahi Kasei Corp | Membrane separation device |
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2004
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Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56121422A (en) * | 1980-02-25 | 1981-09-24 | Yamakuni Tetsukou Kk | Fish preserve apparatus |
| JPS6279898A (en) * | 1985-10-03 | 1987-04-13 | Kubota Ltd | Aeration tank air diffuser |
| JPH06328093A (en) * | 1993-05-27 | 1994-11-29 | Matsushita Electric Works Ltd | Sewage treatment equipment air supply device |
| JPH09131518A (en) * | 1995-11-09 | 1997-05-20 | Hitachi Ltd | Filtration device |
| JPH1094720A (en) * | 1996-09-24 | 1998-04-14 | Kuraray Co Ltd | Hollow fiber membrane module |
| JPH1099882A (en) * | 1996-09-30 | 1998-04-21 | Kubota Corp | Diffuser |
| JP2000157099A (en) * | 1998-11-26 | 2000-06-13 | Mishio Kiko Kk | Rotary air nozzle for culture |
| WO2002004101A1 (en) * | 2000-07-10 | 2002-01-17 | Asahi Kasei Kabushiki Kaisha | Hollow thread film cartridge, hollow thread film module using the cartridge, and tank type filter |
| JP2002336663A (en) * | 2001-05-17 | 2002-11-26 | Japan Organo Co Ltd | Filtration apparatus |
| JP2004008981A (en) * | 2002-06-10 | 2004-01-15 | Asahi Kasei Corp | Membrane separation device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010069361A (en) * | 2008-09-16 | 2010-04-02 | Mitsubishi Rayon Eng Co Ltd | Membrane washing apparatus, membrane separation apparatus, and wastewater treatment apparatus |
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