JP2009028613A - Filtering operation method - Google Patents

Filtering operation method Download PDF

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JP2009028613A
JP2009028613A JP2007194074A JP2007194074A JP2009028613A JP 2009028613 A JP2009028613 A JP 2009028613A JP 2007194074 A JP2007194074 A JP 2007194074A JP 2007194074 A JP2007194074 A JP 2007194074A JP 2009028613 A JP2009028613 A JP 2009028613A
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tank
membrane separation
operation method
water
membrane
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Yasumitsu Miyazaki
泰光 宮崎
Junzo Kobayashi
順三 小林
Katsuhisa Nishijima
克久 西島
Satoshi Terui
聡 照井
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Daicen Membrane Systems Ltd
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Abstract

<P>PROBLEM TO BE SOLVED: To provide a filtering operation method which can maintain stable filtration performance. <P>SOLUTION: The filtering operation method includes a membrane separation process using a membrane module, immersed in a membrane separation tank, at least after a flocculation process in a flocculation tank. In the flocculation process, a flocculant is added to a liquid to be treated in an amount equal to or more than the COD of that of 500-1,000 ppm, to perform flocculation while agitating the liquid at 350-500 r/min for 5-30 minutes by an agitator. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

本発明は、各種分野の水処理に使用できる、浸漬型膜分離装置及びその運転方法に関する。   The present invention relates to a submerged membrane separation apparatus that can be used for water treatment in various fields and an operation method thereof.

各種分野の水処理において、凝集処理と膜分離処理を併用する方法が採用されている。凝集処理後に膜分離処理を行う方法は、凝集処理液に含まれるフロックにより、膜が閉塞され、濾過性能が低下するおそれもある。
特開平１１−３３３４８３号公報 特開２００１−１２９５５７号公報 In water treatment in various fields, a method using a coagulation treatment and a membrane separation treatment in combination is employed. In the method of performing the membrane separation treatment after the agglomeration treatment, the membrane is blocked by the floc contained in the agglomeration treatment liquid, and the filtration performance may be lowered.
Japanese Patent Laid-Open No. 11-333483 JP 2001-129557 A

本発明は、凝集処理と膜分離処理を併用する濾過運転方法であり、膜分離処理の分離能力が高められた濾過運転方法を提供することを課題とする。   It is an object of the present invention to provide a filtration operation method that uses a coagulation treatment and a membrane separation treatment in combination, and has an improved separation ability in the membrane separation treatment.

本発明は、課題の解決手段として、
少なくとも凝集槽における凝集処理工程後に、膜分離槽に浸漬された膜分離モジュールよる膜分離処理工程を有する濾過運転方法であり、
前記凝集処理工程が、被処理液のＣＯＤ５００〜１０００ppmに対して、同等以上の量の凝集剤を添加し、攪拌機により、３５０〜５００ｒ／minで、５〜３０分間攪拌しながら凝集処理する工程である、濾過運転方法を提供する。 As a means for solving the problems, the present invention
It is a filtration operation method having a membrane separation treatment step by a membrane separation module immersed in a membrane separation vessel at least after the aggregation treatment step in the aggregation vessel,
The coagulation treatment step is a step of adding coagulant in an amount equal to or greater than the COD of 500 to 1000 ppm of the liquid to be treated, and coagulating with stirring with a stirrer at 350 to 500 r / min for 5 to 30 minutes. Provided is a filtration operation method.

本発明の濾過運転方法によれば、安定した濾過性能を維持することができる。   According to the filtration operation method of the present invention, stable filtration performance can be maintained.

図１により、本発明の濾過運転方法を説明する。図１は、本発明の濾過運転方法に適した浸漬型膜分離装置の概念図である。図１中の丸で囲まれたＰは、ポンプを示している。   The filtration operation method of the present invention will be described with reference to FIG. FIG. 1 is a conceptual diagram of a submerged membrane separation apparatus suitable for the filtration operation method of the present invention. A circle P in FIG. 1 indicates a pump.

＜浸漬型膜分離装置＞
原水槽１は、原水ライン２１により供給された原水で満たされており、内部にポンプが浸漬されている。原水槽１は、原水供給ライン２２で凝集槽２に接続されている。 <Immersion membrane separator>
The raw water tank 1 is filled with the raw water supplied by the raw water line 21, and a pump is immersed therein. The raw water tank 1 is connected to the aggregation tank 2 by a raw water supply line 22.

凝集槽２は、所定量の凝集剤を添加するための凝集剤添加装置１１、槽内を攪拌するための攪拌機１２、槽内の被処理水のｐＨを調整するためのｐＨ調整装置１３を備えている。凝集槽２の内部にはポンプが浸漬されている。凝集槽２は、凝集処理水ライン２３で膜分離槽３に接続されている。攪拌機１２は、パドル型、プロペラ型等の攪拌羽根（攪拌翼）を有するものである。   The coagulation tank 2 includes a coagulant adding device 11 for adding a predetermined amount of coagulant, an agitator 12 for stirring the inside of the tank, and a pH adjusting device 13 for adjusting the pH of the water to be treated in the tank. ing. A pump is immersed in the aggregation tank 2. The coagulation tank 2 is connected to the membrane separation tank 3 by an aggregation treatment water line 23. The stirrer 12 has a stirring blade (stirring blade) such as a paddle type or a propeller type.

膜分離槽３内は、内部が仕切壁１４により第１槽３ａと第２槽３ｂとに分けられている。第１槽３ａと第２槽３ｂの容積は、同程度であるか、第２槽３ｂの方が大きいことが好ましい。   The inside of the membrane separation tank 3 is divided into a first tank 3 a and a second tank 3 b by a partition wall 14. The volumes of the first tank 3a and the second tank 3b are preferably approximately the same, or the second tank 3b is preferably larger.

仕切壁１４は、膜分離槽３の対向する壁面に両側面が固定されており、下面１４ａは膜分離槽３の底面から離れており、上面１４ｂは満水状態のときに水面よりも下に位置するように設定されている。このため、第１槽３ａと第２槽３ｂは、仕切壁１４の上面（上端）１４ｂ側と下面（下端）１４ａ側にて液の流通が可能なように連通されている。   Both sides of the partition wall 14 are fixed to the opposing wall surfaces of the membrane separation tank 3, the lower surface 14a is separated from the bottom surface of the membrane separation tank 3, and the upper surface 14b is located below the water surface when it is full. It is set to be. For this reason, the 1st tank 3a and the 2nd tank 3b are connected so that the distribution | circulation of the liquid is possible in the upper surface (upper end) 14b side and the lower surface (lower end) 14a side of the partition wall 14. FIG.

第１槽３ａには、槽内を攪拌するための攪拌機１６が備えられており、第２槽３ｂ内には、膜分離モジュール１５が吊り下げられた状態で浸漬されている。膜分離モジュール１５としては、例えば、公知の中空糸膜モジュール（外圧型又は内圧型であるが、好ましくは外圧型）を用いることができる。   The first tank 3a is provided with a stirrer 16 for stirring the inside of the tank, and the membrane separation module 15 is immersed in the second tank 3b in a suspended state. As the membrane separation module 15, for example, a known hollow fiber membrane module (external pressure type or internal pressure type, preferably external pressure type) can be used.

膜分離モジュール１５の直下の第２槽３ｂの底面には、散気装置１７が設置されている。膜分離槽３の底面と一方の側面の境界は、図示するように傾斜面３１となっている。攪拌機１６は、パドル型、プロペラ型等の攪拌羽根（攪拌翼）を有するものである。   An air diffuser 17 is installed on the bottom surface of the second tank 3b immediately below the membrane separation module 15. The boundary between the bottom surface of the membrane separation tank 3 and one side surface is an inclined surface 31 as shown in the figure. The stirrer 16 has a stirring blade (stirring blade) such as a paddle type or a propeller type.

膜分離槽３は、ポンプを備えた透過水ライン２４で透過水槽４に接続され、散気装置１７は、散気ライン２６で空気供給源に接続されている。   The membrane separation tank 3 is connected to the permeated water tank 4 by a permeated water line 24 equipped with a pump, and the air diffuser 17 is connected to an air supply source by an air diffuser line 26.

透過水槽４と膜分離槽３内の膜分離モジュール１５の透過水出口は、ポンプを備えた逆圧洗浄ライン２５で接続されている。   The permeated water outlet of the membrane separation module 15 in the permeated water tank 4 and the membrane separation tank 3 is connected by a back pressure washing line 25 equipped with a pump.

膜分離槽３は、傾斜面３１において汚泥引抜ライン２７で汚泥貯留槽５に接続されている。汚泥引抜ライン２７により、膜分離槽３の底面付近に溜まった汚泥を水とともに汚泥含有水として引き抜くことができる。   The membrane separation tank 3 is connected to the sludge storage tank 5 through a sludge extraction line 27 on the inclined surface 31. The sludge extraction line 27 allows the sludge accumulated near the bottom of the membrane separation tank 3 to be extracted together with water as sludge-containing water.

汚泥貯留槽５内には、図示していない濾過手段（例えば、ＪＩＳ規格で１０メッシュ程度のポリエステルからなる不織布製の濾布が、ステンレス製の枠や籠等の支持体に固定されたもの）が設置されており、汚泥引抜ライン２７から送られた汚泥含有水を汚泥と水に分離する（汚泥を脱水する）。汚泥貯留槽５は、返送ライン２８により、原水槽１に接続されている。   In the sludge storage tank 5, filtration means (not shown) (for example, a non-woven filter cloth made of polyester of about 10 mesh according to JIS standard is fixed to a support such as a stainless steel frame or a basket) The sludge containing water sent from the sludge extraction line 27 is separated into sludge and water (sludge is dehydrated). The sludge storage tank 5 is connected to the raw water tank 1 by a return line 28.

＜浸漬型膜分離装置を用いた濾過運転方法＞
原水が満たされた原水槽１内のポンプを作動させ、原水供給ライン２２から凝集槽２に原水を供給する。 <The filtration operation method using a submerged membrane separator>
The pump in the raw water tank 1 filled with the raw water is operated to supply the raw water from the raw water supply line 22 to the coagulation tank 2.

凝集槽２では、攪拌機１２により槽内を攪拌しながら、凝集剤添加装置１１により、所要量の凝集剤を添加する。このとき、必要に応じてｐＨ調整装置１３により、ｐＨ調整剤を添加してｐＨを９〜１０に調整する。   In the coagulation tank 2, a required amount of coagulant is added by the coagulant adding device 11 while stirring the inside of the tank by the stirrer 12. At this time, a pH adjuster is added by the pH adjuster 13 as necessary to adjust the pH to 9-10.

凝集剤の添加量は、原水のＣＯＤ５００〜１０００ppmに対して、凝集剤の種類に拘わらず同等以上の量である。凝集剤は、例えば、吸着剤、凝結剤、高分子凝集剤等を用いることができる。吸着剤としては、珪藻土、モンモリロナイト、活性白土等の油吸着剤、凝結剤としては、硫酸アルミニウム等の無機化合物、高分子凝集剤としては、アニオン系とカチオン系の高分子凝集剤を挙げることができる。   The addition amount of the flocculant is equal to or greater than the COD of 500 to 1000 ppm of the raw water regardless of the kind of the flocculant. As the flocculant, for example, an adsorbent, a coagulant, a polymer flocculant and the like can be used. Examples of the adsorbent include oil adsorbents such as diatomaceous earth, montmorillonite, and activated clay. Examples of the coagulant include inorganic compounds such as aluminum sulfate. Examples of the polymer flocculant include anionic and cationic polymer flocculants. it can.

攪拌機１２による攪拌は、３５０〜５００ｒ／minで、５〜３０分間行う。   Stirring with the stirrer 12 is performed at 350 to 500 r / min for 5 to 30 minutes.

凝集槽２で凝集処理した処理水は、ポンプを作動させ、ライン２３から膜分離槽３に送る。   The treated water coagulated in the coagulation tank 2 is sent to the membrane separation tank 3 from the line 23 by operating the pump.

次に、膜分離槽３では、第１槽３ａと第２槽３ｂが凝集処理水で満たされた状態で、第１槽３ａでは攪拌機１６で攪拌しながら、第２槽３ｂでは膜分離モジュール１５で濾過する。攪拌機１６による攪拌は、凝集処理工程における攪拌機１２と同様にして行うことが望ましい。   Next, in the membrane separation tank 3, the first tank 3a and the second tank 3b are filled with the agglomerated water, while the first tank 3a is stirred with the stirrer 16, while in the second tank 3b, the membrane separation module 15 is used. Filter with. The stirring by the stirrer 16 is desirably performed in the same manner as the stirrer 12 in the aggregation treatment process.

膜分離モジュール１５による濾過時には、膜面を外側から洗浄するため、散気装置１７から散気することができる。また、適当間隔をおいて、逆圧洗浄ライン２５により、逆圧洗浄することができる。   At the time of filtration by the membrane separation module 15, the membrane surface is washed from the outside, so that air can be diffused from the air diffuser 17. Further, the counter pressure cleaning can be performed by the counter pressure cleaning line 25 at an appropriate interval.

膜分離槽３内の濾過時において、第１槽３ａ内が攪拌機１６で攪拌されているため、第１槽３ａと第２槽３ｂ内の凝集処理水は、仕切壁１４の下面１４ａの下を通り、上面１４ｂを越えて互いに流通する。このため、膜分離槽３内の凝集処理水は、フロックが偏在することなく均一状態になり、分離膜モジュール１５による濾過性能が安定する。   At the time of filtration in the membrane separation tank 3, since the inside of the first tank 3a is agitated by the stirrer 16, the agglomerated water in the first tank 3a and the second tank 3b is below the lower surface 14a of the partition wall 14. And circulates over the upper surface 14b. For this reason, the agglomerated water in the membrane separation tank 3 becomes uniform without flocs being unevenly distributed, and the filtration performance by the separation membrane module 15 is stabilized.

膜分離槽３で濾過した透過水は、透過水ライン２４により、透過水タンク４に送られ、貯水される。透過水タンク４内の透過水は、適宜河川等に放流するほか、膜分離モジュール１５の逆圧洗浄水としても用いられる。   The permeate filtered in the membrane separation tank 3 is sent to the permeate tank 4 through the permeate line 24 and stored. The permeated water in the permeated water tank 4 is appropriately discharged to a river or the like, and is also used as back pressure washing water for the membrane separation module 15.

膜分離槽３の底面付近に溜まったフロック（汚泥）は、汚泥引抜ライン２７から引き抜き、汚泥貯留槽５に送る。汚泥貯留槽５では、汚泥を脱水して、水は原水槽１に返送し、汚泥は廃棄する。   Flock (sludge) collected near the bottom surface of the membrane separation tank 3 is extracted from the sludge extraction line 27 and sent to the sludge storage tank 5. In the sludge storage tank 5, the sludge is dehydrated, the water is returned to the raw water tank 1, and the sludge is discarded.

実施例１
凝集槽２は、高さ０．８５ｍ、幅０．５５ｍ、奥行き０．３３ｍ（容積０．５ｍ３）を用いた。攪拌機１２は、パドル型の長さ０．２ｍの攪拌羽根を有するものを用いた。 Example 1
The agglomeration tank 2 has a height of 0.85 m, a width of 0.55 m, and a depth of 0.33 m (volume 0.5 m 3 ). The stirrer 12 was a paddle type having a stirring blade having a length of 0.2 m.

凝集槽２では、ＣＯＤ５２ppm，ｎヘキサン抽出物量７．６mg／Ｌ、濁度５２、ｐＨ７．３の原水（化粧品工場の排水）に対して、凝集剤（商品名メムフロックＵ００２；ダイセン・メンブレン・システムズ株式会社製）を濃度が８０ppmとなるように添加し、攪拌機１２により、３６０ｒ／minで１０分間、攪拌しながら凝集処理を行った。   In Coagulation Tank 2, coagulant (trade name: Memfloc U002; Daisen Membrane Systems Co., Ltd.) is used for raw water (cosmetic factory effluent) with COD of 52 ppm, n-hexane extract amount of 7.6 mg / L, turbidity of 52, and pH 7.3. Co., Ltd.) was added so that the concentration would be 80 ppm, and agglomeration treatment was performed with the agitator 12 while stirring at 360 r / min for 10 minutes.

膜分離槽３（図１に示す傾斜面３１を有している）は、高さ１．３５ｍ、幅０．６３ｍ、奥行き０．８６ｍ（容積０．８１ｍ３）で、幅方向１／３〜１／２の位置に、高さ１ｍの仕切壁が、上側に０．３５ｍ、下側に０．２５ｍの隙間を空けて、槽の壁に固定されたものを用いた。 The membrane separation tank 3 (having the inclined surface 31 shown in FIG. 1) has a height of 1.35 m, a width of 0.63 m, a depth of 0.86 m (volume 0.81 m 3 ), and 1/3 to 3 in the width direction. A partition wall having a height of 1 m was fixed to the tank wall at a half position with a gap of 0.35 m on the upper side and 0.25 m on the lower side.

膜分離槽３では、攪拌機１６（攪拌機１２と同じもの）により３６０ｒ／minで攪拌しながら、膜分離モジュール（ポリエーテルスルホン中空糸膜を充填したケーシングフリーの浸漬型中空糸膜エレメント〔有効膜面積２．２ｍ２〕を８ユニット組み合わせたもの）により、吸引濾過した。 In the membrane separation tank 3, a membrane separation module (a casing-free submerged hollow fiber membrane element filled with a polyethersulfone hollow fiber membrane [effective membrane area] while being stirred at 360 r / min by a stirrer 16 (the same as the stirrer 12). 2.2 m 2 ] in combination with 8 units).

濾過運転は、散気管１７（パールコン；ダイセン・メンブレン・システムズ社製，PMD-T06）により散気しながら行った。濾過運転３０分ごとに４５秒間の逆圧洗浄をした。   The filtration operation was performed while air was diffused through the air diffuser 17 (Pearlcon; manufactured by Daisen Membrane Systems, Inc., PMD-T06). Backwashing was performed for 45 seconds every 30 minutes during the filtration operation.

濾過運転１時間経過時の透過水は、ＣＯＤ３８ppm、ｎヘキサン抽出物量０．６mg／Ｌ以下、濁度０．２であり、そのまま河川放流ができるものであった。   The permeated water after 1 hour of filtration operation had a COD of 38 ppm, an n-hexane extract amount of 0.6 mg / L or less, and a turbidity of 0.2.

本発明の浸漬型膜分離装置の概念図。The conceptual diagram of the immersion type membrane separation apparatus of this invention.

符号の説明Explanation of symbols

１ 原水槽
２ 凝集槽
３ 膜分離槽
３ａ 第１槽
３ｂ 第２槽
４ 透過水槽
５ 汚泥貯留槽
１１ 凝集剤添加装置
１２ 攪拌機
１４ 仕切壁
１５ 膜分離モジュール

DESCRIPTION OF SYMBOLS 1 Raw water tank 2 Coagulation tank 3 Membrane separation tank 3a 1st tank 3b 2nd tank 4 Permeated water tank 5 Sludge storage tank 11 Coagulant addition apparatus 12 Stirrer 14 Partition wall 15 Membrane separation module

Claims (1)

少なくとも凝集槽における凝集処理工程後に、膜分離槽に浸漬された膜分離モジュールよる膜分離処理工程を有する濾過運転方法であり、
前記凝集処理工程が、被処理液のＣＯＤ５００〜１０００ppmに対して、同等以上の量の凝集剤を添加し、攪拌機により、３５０〜５００ｒ／minで、５〜３０分間攪拌しながら凝集処理する工程である、濾過運転方法。



It is a filtration operation method having a membrane separation treatment step by a membrane separation module immersed in the membrane separation vessel at least after the aggregation treatment step in the aggregation vessel,
The coagulation treatment step is a step of adding coagulant in an amount equal to or greater than the COD of 500 to 1000 ppm of the liquid to be treated, and coagulating with stirring with a stirrer at 350 to 500 r / min for 5 to 30 minutes. There is a filtration operation method.



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JP2014168729A (en) * 2013-03-01 2014-09-18 Swing Corp Water treatment method and water treatment apparatus
JP2017213568A (en) * 2017-09-14 2017-12-07 水ｉｎｇ株式会社 Water treatment method and water treatment device

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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