JP3341427B2 - Immersed membrane device - Google Patents

Immersed membrane device

Info

Publication number
JP3341427B2
JP3341427B2 JP34595693A JP34595693A JP3341427B2 JP 3341427 B2 JP3341427 B2 JP 3341427B2 JP 34595693 A JP34595693 A JP 34595693A JP 34595693 A JP34595693 A JP 34595693A JP 3341427 B2 JP3341427 B2 JP 3341427B2
Authority
JP
Japan
Prior art keywords
membrane
filtration
layer
membrane device
film surface
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
Application number
JP34595693A
Other languages
Japanese (ja)
Other versions
JPH07185270A (en
Inventor
和夫 今井
繁樹 沢田
Original Assignee
栗田工業株式会社
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 栗田工業株式会社 filed Critical 栗田工業株式会社
Priority to JP34595693A priority Critical patent/JP3341427B2/en
Publication of JPH07185270A publication Critical patent/JPH07185270A/en
Application granted granted Critical
Publication of JP3341427B2 publication Critical patent/JP3341427B2/en
Anticipated expiration legal-status Critical
Application status is Expired - Fee Related legal-status Critical

Links

Description

【発明の詳細な説明】 DETAILED DESCRIPTION OF THE INVENTION

【0001】 [0001]

【産業上の利用分野】この発明は、平膜を複数枚積層した積層体や、中空糸膜を平面状、或いはすだれ状にした膜エレメントを複数枚積層した積層体や、管状膜を複数本並行に接続したものを膜ユニットとして用いた浸漬膜装置に関する。 BACKGROUND OF THE INVENTION This invention, laminate or laminated plurality of flat membrane, a hollow fiber membrane flat, or laminate and in which a plurality of laminated films element was interdigital, a plurality of tubular membrane relates submerged membrane device was used connected in parallel as a membrane unit.

【0002】 [0002]

【従来の技術】処理槽の液中に上述した膜ユニットを浸漬し、膜ユニットの内部を吸引して膜を透過した濾過処理水を得る浸漬膜装置は従来から公知である。 BACKGROUND ART immersing the film units described above in a liquid treatment tank, submerged membrane device to obtain the filtered treated water having passed through the membrane by suction the interior of the film unit is known from the prior art. この浸漬膜装置を運転して膜濾過を行った場合、濾過の進行に伴い膜面近傍に高分子溶存物質等の高濃度な濃度分極層、 The submerged membrane when the device was to membrane filtration operation and high concentration concentration polarization layer of polymer dissolved substances on the membrane surface vicinity with the progress of filtration,
或いはこれがゲル状になったゲル層などの非濾過物質が存在するようになると共に、微細な粒子、生物フロック、金属水酸物等の非濾過物質からなるケーク層が膜面に付着する。 Or which together so there is unfiltered material such as a gel layer became gelatinous, fine particles, cake layer composed of biological floes, unfiltered material such as a metal water acid product adheres to the film surface. ケーク層の濾過抵抗の成長速度はゲル層と比較して極めて緩やかであるが、厚い付着層を形成する。 The growth rate of the filtration resistance of the cake layer is a very gentle compared to the gel layer, to form a thick adhesive layer. これらのゲル層やケーク層によって濾過抵抗が生じ、濾過効率が低下する。 Filtration resistance These gel layers and cake layers occurs, filtration efficiency is reduced. そこで、一定時間、膜濾過を行ったら、又は膜濾過運転中に一定濾過圧力になる毎に運転を中止し、膜ユニットに下から気泡を浴びせ膜の間を浮上する気泡と、上向水流とによりゲル層や、ケーク層を膜面から剥離したのち逆洗を行い、濾過性能を回復させる。 Therefore, a certain time, when subjected to membrane filtration, or membrane filtration discontinue operation during operation each time a constant filtration pressure, the bubbles floating between the membrane showered bubbles from below into membrane unit, and an upward water flow gel layer and the performs backwash After peeling off the cake layer from the film surface, to recover the filtration performance. 尚、散気は逆洗の前だけでなく、逆洗の後にも行うことがある。 Incidentally, the air diffuser not only before backwashing, is sometimes performed even after backwashing.

【0003】 [0003]

【発明が解決しようとする課題】しかし、従来は散気によって膜面からゲル層やケーク層を剥離、除去するのに非常に時間がかゝる。 [SUMMARY OF THE INVENTION] However, conventional stripping the gel layer or cake layer from the film surface by the air diffusion, very time or Ru to remove. 従って、散気装置を駆動する動力コストも非常に嵩む。 Therefore, power cost is very increase for driving the air diffuser.

【0004】 [0004]

【課題を解決するための手段】そこで、本発明は、処理槽の液中に膜ユニットを浸漬し、膜を透過した濾過処理水を得る浸漬膜装置において、処理槽内の膜ユニットの下方に直径10mm以上の粗大気泡の散気装置と、 直径 Therefore SUMMARY OF THE INVENTION The present invention provides a membrane unit was immersed in the liquid in the processing tank, the submerged membrane device to obtain a filtration treatment water passed through the membrane, under the membrane units in the processing bath and the air diffuser of the more coarse bubble diameter 10mm, diameter
3mm以下の微細気泡の散気装置を設けたことを特徴とする。 Characterized in that a diffuser below microbubble 3 mm.

【0005】 [0005]

【実施例】図示の実施例において、10は処理槽で、処理槽の液中には膜ユニット11が浸漬してあり、ポンプ12を接続した吸引管13が膜ユニットの内部を吸引し、処理槽内の原液中、膜ユニット11を透過したものを濾過処理水として採水する。 EXAMPLES In the illustrated embodiment, 10 in the treatment tank, is in the liquid in the treatment tank film unit 11 is Yes by dipping, suction tube 13 which connects the pump 12 to aspirate the membrane unit, processing in the stock solution in the tank and water sampling what has passed through the membrane unit 11 as a filtration process water. 膜ユニットは、前述したように平膜の複数枚の積層体、又は中空糸膜を平面状、 Membrane unit, a plurality of stack of flat sheet membrane, as described above, or hollow fiber membrane flat,
或いはすだれ状にした膜エレメントの複数枚の積層体、 Or a plurality of stack of membrane elements you interdigital,
又は管状膜を複数本並行に接続したものである。 Or it is obtained by the tubular film is connected to the plurality of parallel.

【0006】濾過の進行に伴い濾過抵抗を生じさせる前述の濃度分極層ないしゲル層と、ケーク層を気泡により膜面から効果的に剥離すべく、気泡の大きさと、その効果の関係に付いて研究した結果、以下のことが明らかになった。 [0006] and filtered aforementioned concentration polarization layer or gel layer in with cause filtration resistance progression, in order to effectively peeled from the film surface by the bubble cake layer, the size of the bubble, with the relationship of the effect research as a result, it became clear that the following. 先ず濃度分極層ないしゲル層の抑制には、処理槽内の液に膜面沿いの大流速を与えることが効果的であり、それには直径3mm以下の微小気泡による方が効果が高い。 First, the suppression of the concentration polarization layer or gel layer, providing a large flow rate along the film surface in the liquid in the treatment tank is effective, it has the effect is higher for the following microbubbles diameter 3 mm. これは、微小気泡の方がホールドアップ(気泡混合部の気体の割合い)が大きくなり、エアリフト循環流量が増大するためであって、粗大気泡で同じ効果を得るには散気量を大幅に増す必要があり、エネルギー消費が大になる。 This is because the microbubbles (Medical ratio of bubble-mixed portion of the gas) holdup increases, be for the airlift circulation flow rate increases, in order to obtain the same effect coarse bubbles greatly aeration amount There is a need to increase, energy consumption becomes large.

【0007】又、膜面に付着するケーク層を剥離するには、直径10mm以上の粗大気泡を膜面に衝突させることが効果的である。 [0007] Also, in separating the cake layer adhering to the film surface, it is effective impinging more coarse cell diameter 10mm to the film surface. これはケーク層の剥離が気泡の界面での剪断力に起因するため、或る程度大きな気泡でないと剥離に寄与しないからである。 This is because not contribute to peel because due to the shear forces at the interface of the bubble separation of the cake layer, not large bubbles to some extent. 逆にいうと微小な気泡をいくら散気し、膜面に衝突させてもケーク層は剥離しないということである。 Conversely to the air diffuser much fine bubbles, cake layer be allowed to collide with the film surface is that it does not peel. 要するに、微小気泡のみを散気した場合には濃度分極層の抑制には効果的ではあるが、 In short, although when air diffusion only microbubbles in suppression of concentration polarization layer is effective in,
ケーク層を剥離することはできないため濾過抵抗が経時的に増大し、膜面を透過する濾過流速は低下する。 Filtration resistance can not be peeled off the cake layer is increased over time, filtration flow rate passing through the membrane surface is reduced. 又、 or,
粗大気泡のみを散気した場合は膜面流速を与えるためには多大の散気量を必要とし、エネルギーロスが大になる。 If you aeration only coarse bubbles require a great deal of aeration amount to provide a film surface velocity, energy loss becomes large.

【0008】このため、濾過槽内の、膜ユニット11の下方に、膜ユニットの下面全体に気泡を作用させるための散気孔が大きな直径10mm以上の粗大気泡用の散気装置14と、散気孔が小さい直径3mm以下の微小気泡用の散気装置が設けてあり、この実施例では共通のブロワ16で給気するようになっている。 [0008] Therefore, in the filtration tank, below the membrane unit 11, a diffuser 14 for coarse bubble diffusing pores than larger diameter 10mm for applying the bubbles throughout the lower surface of the membrane unit, diffusing pores is provided with a small air diffuser for the following microbubble diameter 3 mm, it adapted to charge air at a common blower 16 in this embodiment.

【0009】従って、膜濾過を一定時間行ったら、又は膜濾過の運転中に一定濾過圧力に達したら、運転を中止し、逆洗を行う前後に、両散気装置14,15を同時に連続的、或いは間欠的に作動するか、 直径3mm以下の Accordingly, when subjected to membrane filtration certain time, or film reaches a predetermined filtration pressure during operation of the filtration, discontinue operation, before and after performing backwashing, simultaneously continuously both diffuser 14 or intermittently operate either below 3mm diameter
微小気泡の散気装置15のみ連続的に作動し、 直径10 Continuously operate only air diffuser 15 of the microbubble diameter 10
mm以上の粗大気泡の散気装置14は間欠的に作動させるか、又は両散気装置14,15を共に間欠的に作動させるが、粗大気泡の散気装置の散気時間を短く(散気の中断間隔を長くすることを含む)するといった具合に両散気装置を運転し、 直径10mm以上の粗大気泡と、 or diffuser 14 mm or more coarse bubbles is intermittently operated, or both diffusers 14 and 15 is intermittently operated together, shortening the air diffusion time of diffuser coarse bubbles (aeration of driving both air diffuser in so on the included) to be prolonged interruption interval, the more coarse bubble diameter 10 mm, straight
径3mm以下の微小気泡を膜ユニットの膜面に作用させ、直径10mm以上の粗大気泡で膜面に付着するケー The following microbubble diameter 3mm to act on the membrane surface of the membrane unit, to adhere to the film surface at a more coarse cell diameter 10mm cable
ク層を効果的に剥離し、膜面に付着するゲル層を直径3 Click layer effectively peeled off, diameter 3 a gel layer adhered to the film surface
mm以下の微小気泡で効果的に剥離する。 mm effectively peeling in the following micro-bubbles. 尚、散気に付いて実施例では膜の運転を中止した後に行う逆洗の前後に行うもので説明したが、これに限らず膜の運転中に常時行うものでもよい。 Although in the embodiment with the diffuser described in those performed before and after the back washing performed after stopping the operation of the film may be configured to perform always during operation of the membrane it is not limited thereto.

【0010】 [0010]

【発明の効果】これにより、最小のエネルギーでもって Effect of the Invention] As a result, with a minimum of energy
膜面に付着するゲル層を直径3mm以 下の微小気泡で The gel layer adheres to the film surface with small bubbles under 3mm diameter than,
ケーク層を直径10mm以上の粗大気泡で、夫々効果的に膜面から剥離し、濾過に寄与する有効膜面積を大きくとれるため膜面を透過する濾過流束を常時、最良の状態に保ち、低エネルギーで濾過を行うことができる。 The cake layer with diameter 10mm or more coarse bubbles, separated from each effectively film surface, constantly filtration flux passing through the effective membrane area can be greatly increased since the film surface contribute to the filtration, keeping the best condition, low it is possible to perform filtration in energy.

【図面の簡単な説明】 BRIEF DESCRIPTION OF THE DRAWINGS

【図1】本発明の一実施例の断面図である。 1 is a cross-sectional view of an embodiment of the present invention.

【符号の説明】 DESCRIPTION OF SYMBOLS

10 処理槽 11 膜ユニット 12 ポンプ 13 吸引管 14 粗大気泡用の散気装置 15 微小気泡用の散気装置 16 ブロワー 10 diffuser 16 blower of the processing vessel 11 film unit 12 pump 13 for the air diffuser 15 microbubbles of the suction pipe 14 for coarse bubbles

Claims (1)

    (57)【特許請求の範囲】 (57) [the claims]
  1. 【請求項1】 処理槽の液中に膜ユニットを浸漬し、膜を透過した濾過処理水を得る浸漬膜装置において、処理槽内の膜ユニットの下方に直径10mm以上の粗大気泡の散気装置と、 直径3mm以下の微細気泡の散気装置を設けたことを特徴とする浸漬膜装置。 1. A membrane unit was immersed in the liquid in the processing tank, the submerged membrane device to obtain a filtration treatment water passed through the membrane, treatment tank membrane unit air diffuser downwardly over the coarse bubble diameter 10mm of When, submerged membrane device characterized by providing the air diffuser of the following fine-bubble diameter 3 mm.
JP34595693A 1993-12-24 1993-12-24 Immersed membrane device Expired - Fee Related JP3341427B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP34595693A JP3341427B2 (en) 1993-12-24 1993-12-24 Immersed membrane device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP34595693A JP3341427B2 (en) 1993-12-24 1993-12-24 Immersed membrane device

Publications (2)

Publication Number Publication Date
JPH07185270A JPH07185270A (en) 1995-07-25
JP3341427B2 true JP3341427B2 (en) 2002-11-05

Family

ID=18380149

Family Applications (1)

Application Number Title Priority Date Filing Date
JP34595693A Expired - Fee Related JP3341427B2 (en) 1993-12-24 1993-12-24 Immersed membrane device

Country Status (1)

Country Link
JP (1) JP3341427B2 (en)

Families Citing this family (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6706189B2 (en) 1998-10-09 2004-03-16 Zenon Environmental Inc. Cyclic aeration system for submerged membrane modules
US7014173B2 (en) 1998-10-09 2006-03-21 Zenon Environmental Inc. Cyclic aeration system for submerged membrane modules
KR100439436B1 (en) 1998-10-09 2004-07-09 제논 인바이런멘탈 인코포레이티드 Cyclic aeration system for submerged membrane modules
US7037426B2 (en) 2000-05-04 2006-05-02 Zenon Environmental Inc. Immersed membrane apparatus
US6863817B2 (en) 2002-12-05 2005-03-08 Zenon Environmental Inc. Membrane bioreactor, process and aerator
CA2605757A1 (en) 2005-04-29 2006-11-09 Siemens Water Technologies Corp. Chemical clean for membrane filter
WO2007022576A1 (en) 2005-08-22 2007-03-01 Siemens Water Technologies Corp. An assembly for water filtration using a tube manifold to minimise backwash
US9587253B2 (en) 2006-02-24 2017-03-07 Toray Industries, Inc. Method of producing chemical product with continuous fermentation and filtering
US9764288B2 (en) 2007-04-04 2017-09-19 Evoqua Water Technologies Llc Membrane module protection
CN101678282B (en) * 2007-05-10 2014-06-25 东丽株式会社 Immersion type membrane separation apparatus and method of operating the same
EP2389998A1 (en) 2007-05-29 2011-11-30 Siemens Industry, Inc. Membrane cleaning with pulsed airlift pump
JP5362343B2 (en) 2008-01-11 2013-12-11 旭化成ケミカルズ株式会社 Membrane separation unit
JP2013500144A (en) 2008-07-24 2013-01-07 シーメンス インダストリー インコーポレイテッドSiemens Industry, Inc. Method and filtration system for providing structural support to a filtration membrane module array in a filtration system
AU2010101488B4 (en) 2009-06-11 2013-05-02 Evoqua Water Technologies Llc Methods for cleaning a porous polymeric membrane and a kit for cleaning a porous polymeric membrane
US9358505B2 (en) 2009-09-03 2016-06-07 General Electric Company Gas sparger for an immersed membrane
AU2011245709B2 (en) 2010-04-30 2015-06-11 Evoqua Water Technologies Llc Fluid flow distribution device
WO2011152461A1 (en) * 2010-06-01 2011-12-08 三菱レイヨン株式会社 Solid-liquid separator device and operation method thereof
WO2012040412A1 (en) 2010-09-24 2012-03-29 Siemens Industry, Inc. Fluid control manifold for membrane filtration system
US10052591B2 (en) * 2010-09-28 2018-08-21 Kolon Industries, Inc. System and method for filtration
US9364805B2 (en) 2010-10-15 2016-06-14 General Electric Company Integrated gas sparger for an immersed membrane
KR101114524B1 (en) * 2011-07-13 2012-02-27 덕인환경주식회사 Air supply device
US8876089B2 (en) 2011-09-15 2014-11-04 Zenon Technology Partnership Method and apparatus to keep an aerator full of air
WO2013048801A1 (en) 2011-09-30 2013-04-04 Siemens Industry, Inc. Improved manifold arrangement
JP2014528354A (en) 2011-09-30 2014-10-27 エヴォクア ウォーター テクノロジーズ エルエルシーEvoqua Water Technologiesllc Isolation valve
US9463419B2 (en) 2012-01-09 2016-10-11 General Electric Company Pulse aeration for immersed membranes
CN104394965B (en) 2012-06-28 2016-11-23 伊沃夸水处理技术有限责任公司 encapsulating method
JPWO2014034836A1 (en) * 2012-08-30 2016-08-08 東レ株式会社 Membrane separation cleaning method for activated sludge
CN104684631A (en) 2012-09-26 2015-06-03 伊沃夸水处理技术有限责任公司 Membrane securement device
US9962865B2 (en) 2012-09-26 2018-05-08 Evoqua Water Technologies Llc Membrane potting methods
US9815027B2 (en) 2012-09-27 2017-11-14 Evoqua Water Technologies Llc Gas scouring apparatus for immersed membranes
AU2014329869B2 (en) 2013-10-02 2018-06-14 Evoqua Water Technologies Llc A method and device for repairing a membrane filtration module
US10322375B2 (en) 2015-07-14 2019-06-18 Evoqua Water Technologies Llc Aeration device for filtration system
US20190039025A1 (en) * 2015-10-08 2019-02-07 Sumitomo Electric Industries, Ltd. Filter unit

Also Published As

Publication number Publication date
JPH07185270A (en) 1995-07-25

Similar Documents

Publication Publication Date Title
ES2358668T3 (en) Procedure for cleaning and maintenance of a membrane surface during filtration.
JP4860843B2 (en) External pressure type hollow fiber membrane module
KR100661935B1 (en) Hollow fiber membrane module, hollow fiber membrane module unit, membrane filtering device using the module unit, and method of operating the membrane filtering device
JP3198923B2 (en) The method of cleaning membrane
WO2001000307A2 (en) Self cleaning filter
JPH06343837A (en) Hollow fiber membrane module
JP3486451B2 (en) The hollow fiber membrane module
JP2946072B2 (en) Filtration method
EP1105205A2 (en) Membrane assembly for solid-liquid separation, method of cleaning the same, and detergent
JP3453173B2 (en) The hollow fiber membrane module with aeration tube
KR20030038658A (en) Hollow thread film cartridge, hollow thread film module using the cartridge, and tank type filter
JPH07313850A (en) Method for backward washing immersion-type ceramic membrane separator
JPH0657302B2 (en) Backwash method of the hollow fiber membrane filter
JPH084722B2 (en) Membrane separation unit
JP2000334276A (en) Operation of filtration device
JP2000189958A (en) Immersion type membrane filter device
JP2001190937A (en) Water purification equipment and method of cleaning membrane element
EP0125192B1 (en) Plant and method for treating swimming pool water by means of a membrane separation apparatus
JPH10286441A (en) Cleaning method of hollow yarn membrane module and filtration device used for the method
JP2001205055A (en) Method for operating membrane separation apparatus and apparatus therefor
US20020162784A1 (en) Membrane separator
WO1999029630A1 (en) Apparatus and method for treating water
CN1612778A (en) Membrane separation device and membrane separation method
JP3446399B2 (en) Submerged membrane separator and a membrane separation method using the same
JP2001017970A (en) Water treatment equipment using immersion type membrane filtration device

Legal Events

Date Code Title Description
FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20080823

Year of fee payment: 6

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20090823

Year of fee payment: 7

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20090823

Year of fee payment: 7

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20100823

Year of fee payment: 8

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20110823

Year of fee payment: 9

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20120823

Year of fee payment: 10

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20130823

Year of fee payment: 11

LAPS Cancellation because of no payment of annual fees