JP2007167779A - Method for treating waste water - Google Patents

Method for treating waste water Download PDF

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JP2007167779A
JP2007167779A JP2005370007A JP2005370007A JP2007167779A JP 2007167779 A JP2007167779 A JP 2007167779A JP 2005370007 A JP2005370007 A JP 2005370007A JP 2005370007 A JP2005370007 A JP 2005370007A JP 2007167779 A JP2007167779 A JP 2007167779A
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filtration
aeration
back pressure
filtration operation
pressure washing
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Toyozo Hamada
豊三 浜田
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Daicel Corp
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Daicel Chemical Industries Ltd
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  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for treating waste water, in which the filtration capacity (a water permeation speed) of the filtration membrane is increased by improving a method for operating a filtration membrane. <P>SOLUTION: The method for treating waste water, in which a waste water treatment apparatus provided with: a treatment tank having the filtration membrane and an air diffusion pipe; and a flocculant throwing means for throwing a flocculant in the treatment tank is used to perform flocculation, filtration and back pressure washing, comprises a step of: removing a suspended component from the lower part of the treatment tank after air diffusion from the air diffusion pipe is stopped during the time to operate the filtration membrane or during the time to subject the filtration membrane to back pressure washing. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

本発明は、含油排水の処理に適した排水処理方法に関する。   The present invention relates to a wastewater treatment method suitable for treating oil-containing wastewater.

水資源の有効利用への関心の高まりと共に、大量に水道水を消費する洗車場などの洗浄水（１台当たり１５０Ｌ以上必要）に対する節水の要望と、その一方で排水をそのまま垂れ流すことに対する水質汚染への懸念が大きくなっている。特に洗車場で生じる排水には、土砂と共にワックス等の油分だけでなく、界面活性剤が含まれている。界面活性剤は自然分解されにくいために、河川、湖沼の環境汚染に繋がる。そこで、洗車排水を処理し、処理水を洗車用水として再利用することで、上記課題を解決しようとする試みがなされている。
特開２００３−１７０００７号公報 特開２００３−３２６１０５号公報 特開２００３−３２７０９３号公報 特開平９−７５６９１号公報 特開平９−１４１０６５号公報 Along with increasing interest in effective use of water resources, demand for water saving for washing water (150L or more per car) that consumes a large amount of tap water, and water quality for dripping down the drainage as it is Concerns about pollution are growing. In particular, the wastewater generated at the car wash station contains not only oil such as wax but also surfactant as well as earth and sand. Surfactants are not easily decomposed naturally, leading to environmental pollution of rivers and lakes. Then, the trial which tries to solve the said subject is made | formed by processing car wash wastewater and reusing treated water as car wash water.
JP 2003-170007 A JP 2003-326105 A JP 2003-327093 A Japanese Patent Laid-Open No. 9-75691 Japanese Patent Laid-Open No. 9-14165

洗車場等に設置される排水処理装置は、設置場所の制約から、装置自体を小さなものにせざるを得ず、処理量（透水速度）を増大させることは困難である。このため、濾過運転方法の改善により、装置の濾過能力を最大限発揮させることで、処理量透水速度）を増大させることが考えられる。   A wastewater treatment device installed in a car wash or the like must be made small due to restrictions on the installation location, and it is difficult to increase the treatment amount (water permeability rate). For this reason, it is conceivable to increase the throughput (transmission rate) by maximizing the filtration capacity of the apparatus by improving the filtration operation method.

本発明は、濾過運転方法の改善により、濾過能力（透水速度）を増大させることができる排水処理方法を提供することを課題とする。   An object of the present invention is to provide a wastewater treatment method capable of increasing the filtration capacity (water transmission rate) by improving the filtration operation method.

本発明は、課題の解決手段として、
濾過膜及び散気管を備えた処理槽と、前記処理槽に凝集剤を投入する凝集剤投入手段を有する排水処理装置を用い、凝集、濾過及び逆圧洗浄をする排水処理方法であり、
前記濾過膜による濾過運転中又は逆圧洗浄中に前記散気管からの散気を停止した後、前記処理槽の下部から懸濁成分を除去する排水処理方法を提供する。 As a means for solving the problems, the present invention
A wastewater treatment method using a wastewater treatment apparatus having a treatment tank equipped with a filtration membrane and an air diffuser and a flocculant charging means for charging a flocculant into the treatment tank, and performing agglomeration, filtration and back pressure washing,
Provided is a wastewater treatment method for removing suspended components from the lower part of the treatment tank after stopping the aeration from the aeration tube during the filtration operation by the filtration membrane or the back pressure washing.

本発明の排水処理方法によれば、散気を停止した状態で懸濁物質（スラッジ等）を取り除く方法であるため、濾過運転に影響を与えることなく、効率よく懸濁物質（スラッジ等）を取り除くことができる。このため、長期間、高い透水速度で濾過運転することができる。   According to the wastewater treatment method of the present invention, the suspended solids (sludge etc.) are removed efficiently without affecting the filtration operation because the suspended solids (sludge etc.) are removed in the state where the aeration is stopped. Can be removed. For this reason, it is possible to perform a filtration operation at a high water transmission rate for a long period of time.

＜排水処理装置＞
図１は、本発明の排水処理方法に適した排水処理装置の概念図である。 <Effluent treatment device>
FIG. 1 is a conceptual diagram of a wastewater treatment apparatus suitable for the wastewater treatment method of the present invention.

排水処理装置１０は、凝集機能と濾過機能を備えた処理槽１１と、処理槽１１の外に設置された凝集剤投入装置２０を有している。   The waste water treatment apparatus 10 includes a treatment tank 11 having a coagulation function and a filtration function, and a flocculant charging apparatus 20 installed outside the treatment tank 11.

処理槽１１は、中央部に配置された仕切板１３により、互いに液の流通が可能なように凝集反応槽１４と濾過槽１５に区画されている。   The treatment tank 11 is divided into an agglomeration reaction tank 14 and a filtration tank 15 by a partition plate 13 disposed in the center so that liquids can flow through each other.

仕切板１３は、処理槽１１の側壁に固定されており、処理槽１１の底面１１ａには接していない。仕切板１３の上面の高さは、処理槽１１内の側壁の高さよりも低く、濾過運転時には、被処理液の水面よりも低くなるように調整されている。その結果、被処理液は、仕切板１３の上下から、凝集反応槽１４と濾過槽１５を自由に流通循環する。なお、仕切板１３は、被処理液の性状及び凝集剤の種類に応じて、大きさや設置位置を自由に調整できる。   The partition plate 13 is fixed to the side wall of the processing tank 11 and is not in contact with the bottom surface 11 a of the processing tank 11. The height of the upper surface of the partition plate 13 is adjusted to be lower than the height of the side wall in the processing tank 11 and lower than the water surface of the liquid to be processed during the filtration operation. As a result, the liquid to be treated freely circulates through the aggregation reaction tank 14 and the filtration tank 15 from above and below the partition plate 13. Note that the size and installation position of the partition plate 13 can be freely adjusted according to the properties of the liquid to be treated and the type of the flocculant.

凝集反応槽１４には、定量フィーダ付きの凝集剤投入装置２０が接続されており、必要に応じて攪拌装置も付設することができる。   The aggregating reaction tank 14 is connected with an aggregating agent feeding device 20 with a quantitative feeder, and a stirring device can be attached if necessary.

凝集剤としては、無機凝集剤と有機凝集剤の混合物が好ましい。無機凝集剤としては、ベントナイト、ポリ塩化アルミニウム、硫酸アルミニウム、ポリ塩化鉄等が好ましく、有機凝集剤としては、ポリアクリルアミド、ポリ（メタ）アクリル酸、多糖類等の水溶性高分子が好ましい。凝集剤は、無機凝集剤を９０質量％以上含有するものが好ましく、残部は有機凝集剤を用いることができる。   As the flocculant, a mixture of an inorganic flocculant and an organic flocculant is preferable. As the inorganic flocculant, bentonite, polyaluminum chloride, aluminum sulfate, polyiron chloride and the like are preferable, and as the organic flocculant, water-soluble polymers such as polyacrylamide, poly (meth) acrylic acid and polysaccharides are preferable. The flocculant preferably contains 90% by mass or more of an inorganic flocculant, and the remainder can be an organic flocculant.

より好ましい凝集剤としては、ベントナイト４０〜５０質量％、硫酸アルミニウム４０〜５０質量％、アルギン酸ナトリウム０〜１０質量％、カチオン系アクリルアミド０〜１０質量％を含むもの（但し、ベントナイトと硫酸アルミニウムの合計が９０質量％以上）を挙げることができる。   More preferable flocculants include bentonite 40 to 50% by mass, aluminum sulfate 40 to 50% by mass, sodium alginate 0 to 10% by mass, and cationic acrylamide 0 to 10% by mass (however, the sum of bentonite and aluminum sulfate) Is 90% by mass or more).

濾過槽１５には、外圧型濾過膜１２が浸漬されており、外圧型濾過膜１２直下の底面１１ａには、散気管２１が設置されている。濾過槽１５に至るライン３１には、薬剤注入ユニット２３を接続することができる。   An external pressure filtration membrane 12 is immersed in the filtration tank 15, and an air diffuser 21 is installed on the bottom surface 11 a immediately below the external pressure filtration membrane 12. A drug injection unit 23 can be connected to the line 31 leading to the filtration tank 15.

濾過槽１５内に浸漬された、吸引手段により濾過可能な外圧型濾過膜１２としては、公知の分離膜を用いることができるが、酢酸セルロース製の中空糸膜が好ましい。なお、濾過可能であれば、吸引手段（図１のポンプ２６）に限定されず、同等の機能を発揮するもの、例えば、吸引とは逆に圧力を送り込む方式のものでもよい。   A known separation membrane can be used as the external pressure filtration membrane 12 immersed in the filtration tank 15 and can be filtered by suction means, but a hollow fiber membrane made of cellulose acetate is preferable. In addition, as long as it can be filtered, it is not limited to the suction means (pump 26 in FIG. 1), and may exhibit an equivalent function, for example, a system that sends pressure opposite to suction.

散気管２１は、散気管自体を処理槽１１の外に設置して、気泡供給口のみを装置内に設置してもよい。散気管２１は、直径が１〜２０ｍｍの範囲の大きさの気泡を発生できるものが好ましい。   For the air diffuser 21, the air diffuser itself may be installed outside the processing tank 11, and only the bubble supply port may be installed in the apparatus. The air diffuser 21 is preferably capable of generating bubbles having a diameter in the range of 1 to 20 mm.

＜排水処理方法＞
次に、図１に示す排水処理装置１０を用いた排水処理方法を説明する。 <Wastewater treatment method>
Next, a wastewater treatment method using the wastewater treatment apparatus 10 shown in FIG. 1 will be described.

まず、ポンプ２５を作動させて、被処理液供給ライン３０から、原水乃至一次処理水を凝集反応槽１４内に供給する。   First, the pump 25 is operated to supply raw water or primary treated water into the aggregation reaction tank 14 from the liquid supply line 30 to be treated.

処理対象水が、洗車場等で生じた洗車排水であれば、油や界面活性剤と共に砂、小石、ゴミが含まれていることがあるため、予めこれらを取り除いたものを原水乃至一次処理水とすることができる。   If the water to be treated is car wash wastewater generated at a car wash, etc., it may contain sand, pebbles, and dust along with oil and surfactants. It can be.

凝集反応槽１４では、凝集剤投入装置２０から所定量の凝集剤を添加した後、好ましくは十分に攪拌し、液が凝集反応槽１４と濾過槽１５内を循環するようにしてフロックを形成、沈降させる。濾過槽１５では、吸引ポンプ２６を作動させ、凝集反応槽１４での凝集反応と並行して外圧型濾過膜１２で濾過処理する。なお、膜の孔径が大きく、濾過抵抗が十分に小さい場合、重力差のみで濾過が可能となる。   In the agglomeration reaction tank 14, after adding a predetermined amount of the aggregating agent from the aggregating agent charging device 20, it is preferably sufficiently stirred to form a flock so that the liquid circulates in the agglomeration reaction tank 14 and the filtration tank 15. Allow to settle. In the filtration tank 15, the suction pump 26 is operated to perform filtration with the external pressure filtration membrane 12 in parallel with the aggregation reaction in the aggregation reaction tank 14. In addition, when the pore diameter of the membrane is large and the filtration resistance is sufficiently small, filtration is possible only by the difference in gravity.

このようにして、凝集反応槽１４と濾過槽１５で液を循環させることにより、凝集反応と濾過が並行して進行する。濾過槽１５での処理後、処理水は、ライン３１から次の処理部（例えば、活性炭処理部）又は貯水タンクに送る。   In this manner, the liquid is circulated in the agglomeration reaction tank 14 and the filtration tank 15, so that the agglutination reaction and the filtration proceed in parallel. After the treatment in the filtration tank 15, the treated water is sent from the line 31 to the next treatment unit (for example, activated carbon treatment unit) or a water storage tank.

一定時間の濾過運転後、運転を停止し、ライン３１から送られた洗浄水（処理水又は水道水）に対して、薬剤注入ユニット２３から次亜塩素酸ナトリウム水溶液等を供給した薬液により、濾過膜１２の逆圧洗浄をすることもできる。逆圧洗浄時には、洗浄能力を高めるため、散気管２１から散気することが好ましい。逆圧洗浄中、常に散気することが好ましいが、逆圧洗浄過程の一部では、散気を散気することも可能である。   After the filtration operation for a certain time, the operation is stopped, and the washing water (treated water or tap water) sent from the line 31 is filtered by a chemical solution supplied with a sodium hypochlorite aqueous solution or the like from the chemical injection unit 23. The membrane 12 can also be back-pressure cleaned. At the time of back pressure cleaning, it is preferable that air is diffused from the air diffuser 21 in order to enhance the cleaning performance. It is preferable to always diffuse during the counter pressure cleaning, but it is also possible to diffuse the aeration during part of the counter pressure cleaning process.

本発明の排水処理方法では、濾過膜１２による濾過運転過程の全部又は一部、或いは逆圧洗浄過程の一部において、散気管２１による散気を停止して、処理槽１１の底部に接続された引き抜きライン３２、３３から懸濁成分を抜き取る。このような処理方法としては、下記の（ａ）〜（ｄ）の方法を例示することができる。ここで「散気を停止して」には、濾過運転中に散気は行わず、逆圧洗浄開始時に散気を開始する場合も含む。   In the wastewater treatment method of the present invention, in the whole or a part of the filtration operation process by the filtration membrane 12 or in the part of the back pressure washing process, the aeration by the aeration tube 21 is stopped and connected to the bottom of the treatment tank 11. The suspended components are extracted from the drawn lines 32 and 33. Examples of such treatment methods include the following methods (a) to (d). Here, “stop the aeration” includes the case where the aeration is not performed during the filtration operation and the aeration is started at the start of the back pressure cleaning.

（ａ）(1)濾過運転開始（散気停止）→濾過運転（散気停止）→濾過運転停止・濾過膜の逆圧洗浄（逆圧洗浄中に散気）
(2)→濾過運転再開（散気停止）→……
方法（ａ）は、濾過運転中は散気を停止して、逆圧洗浄時にのみ散気する方法である。即ち、逆圧洗浄の開始直前は散気が停止されている。 (A) (1) Filtration operation start (aeration stop) → Filtration operation (aeration stop) → Filtration operation stop / back pressure washing of filtration membrane (aeration during back pressure washing)
(2) → Restart filtration operation (stop aeration) → ……
The method (a) is a method in which the aeration is stopped during the filtration operation and the aeration is performed only at the time of back pressure cleaning. That is, aeration is stopped immediately before the start of back pressure cleaning.

（ｂ）(1)濾過運転開始（散気開始）→濾過運転（散気中）→濾過運転（散気停止）→濾過運転（散気再開）→濾過運転停止・濾過膜の逆圧洗浄（逆圧洗浄中に散気）
(2)→濾過運転再開（散気開始）→……
方法（ｂ）は、濾過運転中、適当間隔で、適当な回数、散気したり、散気しなかったりする方法であるが、逆圧洗浄の開始直前には散気されている。 (B) (1) Filtration operation start (aeration start) → Filtration operation (aeration) → Filtration operation (aeration stop) → Filtration operation (aeration restart) → Filtration operation stop / back pressure washing of the filter membrane ( Air diffused during backwashing)
(2) → Resume filtration operation (start aeration) → ……
Method (b) is a method in which air is diffused or not diffused at an appropriate interval during filtration operation, but air is diffused immediately before the start of back pressure cleaning.

（ｃ）(1)濾過運転開始（散気開始）→濾過運転（散気中）→濾過運転（散気停止）→濾過運転停止・濾過膜の逆圧洗浄（逆圧洗浄中に散気）
(2)→濾過運転再開（散気開始）→……
方法（ｃ）は、散気中の状態から、逆圧洗浄開始の直前までに散気を停止する方法である。即ち、逆圧洗浄の開始直前は散気が停止されている。 (C) (1) Filtration operation start (aeration start) → Filtration operation (aeration) → Filtration operation (aeration stop) → Filtration operation stop / back pressure washing of filtration membrane (aeration during back pressure washing)
(2) → Resume filtration operation (start aeration) → ……
Method (c) is a method of stopping the aeration from the state during the aeration until just before the start of the reverse pressure cleaning. That is, aeration is stopped immediately before the start of back pressure cleaning.

（ｄ）(1)濾過運転開始（散気停止）→濾過運転（散気開始）→濾過運転停止・濾過膜の逆圧洗浄（散気停止）→逆圧洗浄（散気再開）
(2)→濾過運転再開（散気停止）→……
方法（ｄ）は、逆圧洗浄の開始直後に散気を停止するが、逆圧洗浄の途中で散気を再開する方法である。なお、逆圧洗浄時の全部で散気を停止してもよい。 (D) (1) Filtration operation start (aeration stop) → Filtration operation (aeration start) → Filtration operation stop / filtration membrane back pressure washing (aeration stop) → back pressure washing (aeration restart)
(2) → Restart filtration operation (stop aeration) → ……
Method (d) is a method in which the aeration is stopped immediately after the start of the back pressure cleaning, but the aeration is resumed in the middle of the back pressure cleaning. In addition, you may stop aeration in the whole at the time of back pressure washing | cleaning.

（ａ）〜（ｄ）のいずれの処理方法においても、濾過運転時間（濾過開始から逆圧洗浄までの時間）は約１０〜６０分間で、逆圧洗浄時間は約０．５〜２分間であり、散気の停止時間は、少なくとも１つの運転サイクル（濾過運転開始から逆圧洗浄終了までを１サイクルとする。）中、２〜６０分間、好ましくは２〜３０分間である。   In any of the treatment methods (a) to (d), the filtration operation time (time from the start of filtration to back pressure washing) is about 10 to 60 minutes, and the back pressure washing time is about 0.5 to 2 minutes. The aeration stop time is 2 to 60 minutes, preferably 2 to 30 minutes, in at least one operation cycle (one cycle from the start of filtration operation to the end of back pressure washing).

懸濁成分の抜き取りは、散気停止中の所望時に行うが、散気停止中に必ず抜き取り処理をする必要はない。例えば、各方法とも１つの運転サイクル（濾過運転開始から逆圧洗浄終了までを１サイクルとする。）を繰り返すものであるが、処理方法や懸濁成分の沈殿状況に応じて、１サイクル又は複数サイクルに１回以上の抜き取りをすることができる。   The suspension component is extracted at a desired time while the aeration is stopped, but it is not always necessary to perform the extraction process while the aeration is stopped. For example, each method repeats one operation cycle (one cycle from the start of filtration operation to the end of backwashing), but one or more cycles depending on the treatment method and the state of sedimentation of suspended components. One or more extractions can be made per cycle.

例えば、方法（ｂ）、（ｃ）における懸濁成分の抜き取りは、濾過運転途中に散気を開始するとき（即ち、散気停止状態から散気を開始するとき）、散気開始前又は散気開始後に行うことができる。なお、ここでいう「散気の開始」は、運転開始時から初めて散気をする場合と、一旦散気を停止した後に散気を再開する場合を含む。   For example, the extraction of the suspended components in the methods (b) and (c) can be performed when aeration is started during the filtration operation (that is, when aeration is started from a state where the aeration is stopped), before the start of the aeration, or before the aeration. This can be done after starting qi. Here, “starting of air diffusion” includes a case where air is diffused for the first time from the start of operation and a case where air diffusion is resumed after the air diffusion is once stopped.

懸濁成分の抜き取りを散気開始前に行うときは、散気停止状態の全時間の内、散気停止時間の内、最後の２０％以内の時間帯域に行うことが好ましく、１０％以内の時間帯域に行うことがより好ましく、散気開始直前（即ち、抜き取り終了後、直ちに散気が開始される）に行うことが特に好ましい。   When the suspension component is extracted before the start of aeration, it is preferably performed within the last 20% of the aeration stop time within the total time of the aeration stop state, preferably within 10%. It is more preferable to carry out in the time zone, and it is particularly preferable to carry out immediately before the start of the aeration (that is, the aeration starts immediately after completion of the extraction).

懸濁成分の抜き取りを散気開始後に行うときは、散気開始後から１分以内に行うことが好ましく、散気開始直後（即ち、散気開始後、直ちに抜き取りが開始される）に行うことがより好ましい。   When the suspension component is extracted after the start of the aeration, it is preferably performed within 1 minute after the start of the aeration, and immediately after the start of the aeration (that is, the extraction starts immediately after the start of the aeration). Is more preferable.

例えば、方法（ａ）、（ｃ）における懸濁成分の抜き取りは、濾過膜の逆圧洗浄をするとき、逆圧洗浄開始前の濾過運転中に散気を停止した状態で行うことができる。懸濁成分の抜き取りを逆圧洗浄の開始前に行うときは、濾過開始から逆圧洗浄開始までの全時間の内、最後の２０％以内の時間帯域に行うことが好ましく、１０％以内の時間帯域に行うことがより好ましく、逆圧洗浄の開始直前（即ち、抜き取り終了後、直ちに逆圧洗浄が開始される）に行うことが特に好ましい。   For example, the extraction of suspended components in the methods (a) and (c) can be performed in a state where the aeration is stopped during the filtration operation before the start of the reverse pressure washing when the filtration membrane is back pressure washed. When the suspension component is extracted before the start of backwashing, it is preferably performed within the last 20% of the total time from the start of filtration to the start of backwashing, and the time within 10% It is more preferable to perform in the zone, and it is particularly preferable to perform it immediately before the start of the back pressure cleaning (that is, the back pressure cleaning is started immediately after completion of the extraction).

例えば、方法（ｄ）における懸濁成分の抜き取りは、濾過膜の逆圧洗浄をするとき、逆圧洗浄開始後の逆圧洗浄中に散気を停止した状態で行うことができる。逆圧洗浄の開始後から１分以内に行うことが好ましく、逆圧洗浄の開始直後（即ち、逆圧洗浄の開始とほぼ同時に抜き取りが開始される）に行うことがより好ましい。   For example, in the method (d), the suspension component can be extracted in a state where the aeration is stopped during the back pressure cleaning after the start of the back pressure cleaning when the back filtration of the filtration membrane is performed. It is preferably performed within 1 minute after the start of back pressure cleaning, and more preferably immediately after the start of back pressure cleaning (that is, extraction is started almost simultaneously with the start of back pressure cleaning).

このように散気の停止と懸濁成分の抜き取りを関連づけることにより、懸濁成分を処理槽の底に滞留させた状態にて抜き取ることができるようになるため、より短い時間でより多量の懸濁成分を除去できる。   By associating the stop of the aeration and the extraction of the suspended components in this way, the suspended components can be extracted while remaining in the bottom of the treatment tank. Turbid components can be removed.

なお、方法（ａ）のように、濾過運転中に散気されず、逆圧洗浄時のみ散気され、逆圧洗浄の開始直前に懸濁成分の抜き取りが行われる場合は、最も懸濁成分の除去効率（懸濁成分の抜き取りに要する時間当たりの懸濁成分の抜き取り量）が大きい。   In addition, as in the method (a), when the air is not diffused during the filtration operation but is diffused only at the time of back pressure washing, and the suspended component is extracted immediately before the start of the back pressure washing, the most suspended component The removal efficiency (the amount of the suspended component extracted per time required for extracting the suspended component) is large.

本発明の排水処理方法は、ｎ−ヘキサン抽出物質が１ｍｇ／Ｌを超える量含有された含油排水の処理に適しており、更にｎ−ヘキサン抽出物質が１ｍｇ／Ｌを超える量、ＣＯＤ濃度が１０ｍｇ／Ｌを超える数値、ＳＳ（濁質）濃度が１０ｍｇ／Ｌを超える数値である含油排水の処理に適しており、特に洗車場等で生じる油や界面活性剤を含む含油有排水の処理に適している。   The wastewater treatment method of the present invention is suitable for the treatment of oil-containing wastewater containing n-hexane extract in an amount exceeding 1 mg / L, and the n-hexane extract is in an amount exceeding 1 mg / L and the COD concentration is 10 mg. Suitable for the treatment of oil-containing wastewater with a value exceeding / L and SS (turbidity) concentration exceeding 10 mg / L, especially suitable for the treatment of oil-containing wastewater containing oil and surfactants generated at car wash stations, etc. ing.

実施例１
図１に示す排水処理装置１０を用いて、上記した（ａ）の処理方法により、排水処理をした。 Example 1
Using the waste water treatment apparatus 10 shown in FIG. 1, waste water treatment was performed by the above-described treatment method (a).

内容積0.76m３の処理槽１１の中央部に仕切り板１３を設置し、濾過槽１５の底部に散気管（パールコン：ダイセン・メンブレン・システムズ社製、PMD-T06）２１を２本設置し、その真上に、外径２mm、内径０．９mmの酢酸セルロース中空糸膜を充填したケーシングフリーの浸漬型膜エレメント（濾過膜１２）３m２を９０ｍｍ間隔で６ユニット浸漬配置させた。 A partition plate 13 is installed at the center of the processing tank 11 having an internal volume of 0.76 m 3 , and two aeration tubes (Pearlcon: manufactured by Daisen Membrane Systems, Inc., PMD-T06) 21 are installed at the bottom of the filtration tank 15. Immediately above, 3 units of 3 m 2 of a casing-free submerged membrane element (filtration membrane 12) filled with a cellulose acetate hollow fiber membrane having an outer diameter of 2 mm and an inner diameter of 0.9 mm was disposed so as to be immersed at 90 mm intervals.

被処理液として、洗車排水（平均ｎ−ヘキサン抽出物量１６mg/L、平均COD濃度４２mg/L、濁質（SS）濃度４８mg/L）を油水分離槽から処理槽１１に導いた。   Car wash wastewater (average n-hexane extract amount 16 mg / L, average COD concentration 42 mg / L, turbidity (SS) concentration 48 mg / L) was introduced from the oil / water separation tank to the treatment tank 11 as the liquid to be treated.

凝集剤供給装置２０から凝集剤〔ベントナイト４８質量％、硫酸アルミニウム４８質量％、アルギン酸ナトリウム２質量％、カチオン系ポリアクリルアミド２質量％である、商品名メムフロック（ダイセル化学工業株式会社製）〕を５０mg/L添加して、凝集反応と吸引濾過を同時に行い、（ａ）の処理法を適用して図２に示す運転条件にて濾過運転を行った（ＯＮは散気中、ＯＦＦは散気停止）。濾過液は濾過液タンクに貯蔵して、一部は逆洗水として使用し、残りは洗車排水再利用水として、活性炭を通水させた後に洗車機に戻した。   50 mg of flocculant [Brandite 48% by mass, aluminum sulfate 48% by mass, sodium alginate 2% by mass, cationic polyacrylamide 2% by mass, Memflock (manufactured by Daicel Chemical Industries, Ltd.)] / L was added, and agglomeration reaction and suction filtration were performed at the same time, and the filtration operation was performed under the operating conditions shown in FIG. 2 by applying the processing method (a) (ON is aeration, OFF is aeration stop) ). Filtrate was stored in a filtrate tank, a part was used as backwash water, and the rest was used as car wash wastewater reused water.

濾過時間は１５分、逆圧洗浄は、有効塩素濃度５mg/Lによる次亜塩素酸ナトリウム水溶液により１分間行い、散気は逆圧洗浄時のみ、４m３／Hrで１分間行った。散気停止中における引き抜きライン３２、３３からの懸濁成分の抜き取りは、運転サイクル１回ごとに１回の割合で逆圧洗浄の開始直前に行った。１回の抜き取りに要した時間は約１０秒間であった。懸濁成分の抜き取り終了後、直ちに逆圧洗浄を開始した。 Filtration time was 15 minutes, back pressure washing was performed with sodium hypochlorite aqueous solution with an effective chlorine concentration of 5 mg / L for 1 minute, and aeration was performed at 4 m 3 / Hr for 1 minute only during back pressure washing. The suspension components were extracted from the drawing lines 32 and 33 during the stop of the aeration immediately before the start of the back pressure washing at a rate of once per operation cycle. The time required for one extraction was about 10 seconds. Immediately after the suspension component was removed, back pressure washing was started.

実施例１の濾過運転開始時の透水速度は０．８ｍ／日であり、６ヶ月経過後の透水速度も０．８ｍ／日であった。このように短時間で効率よくスラッジを抜き取ることができるため、長期間、安定した濾過運転をすることができた。   The water transmission rate at the start of the filtration operation of Example 1 was 0.8 m / day, and the water transmission rate after 6 months was also 0.8 m / day. Since sludge can be efficiently extracted in a short time as described above, a stable filtration operation can be performed for a long time.

実施例２
（ｂ）の処理法を適用し、実施例１と同様にして、図２に示す運転条件にて濾過運転を行った（ＯＮは散気中、ＯＦＦは散気停止）。 Example 2
By applying the treatment method (b), the filtration operation was performed in the same manner as in Example 1 under the operation conditions shown in FIG. 2 (ON is aeration, OFF is the aeration stop).

濾過時間は１５分、逆圧洗浄は、有効塩素濃度５mg/Lによる次亜塩素酸ナトリウム水溶液による逆洗を１分間行った。散気は４m３／Hrで、濾過運転開始から逆圧洗浄終了までの合計の散気停止時間は５分間であった。散気停止中における引き抜きライン３２、３３からの懸濁成分に抜き取りは、運転サイクル１回ごとに１回の割合で行った。１回の抜き取りに要した時間は約１０秒間であった。 The filtration time was 15 minutes, and the back pressure washing was performed for 1 minute with a sodium hypochlorite aqueous solution with an effective chlorine concentration of 5 mg / L. The aeration was 4 m 3 / Hr, and the total aeration stop time from the start of the filtration operation to the end of the back pressure washing was 5 minutes. Extraction of the suspended components from the drawing lines 32 and 33 during the aeration stop was performed at a rate of once per operation cycle. The time required for one extraction was about 10 seconds.

実施例２の濾過運転開始時の透水速度は０．８ｍ／日であり、３ヶ月経過後の透水速度は０．７ｍ／日であった。このように短時間で効率よくスラッジを抜き取ることができるため、長期間、安定した濾過運転をすることができた。   The water transmission rate at the start of the filtration operation of Example 2 was 0.8 m / day, and the water transmission rate after 3 months was 0.7 m / day. Since sludge can be efficiently extracted in a short time as described above, a stable filtration operation can be performed for a long time.

実施例３
（ｃ）の処理法を適用し、実施例１と同様にして、図２に示す運転条件にて濾過運転を行った（ＯＮは散気中、ＯＦＦは散気停止）。 Example 3
The treatment method (c) was applied, and a filtration operation was performed under the operation conditions shown in FIG. 2 in the same manner as in Example 1 (ON is aeration, OFF is aeration stop).

濾過時間は１５分、逆圧洗浄は、有効塩素濃度５mg/Lによる次亜塩素酸ナトリウム水溶液による逆洗を１分間行った。散気は４m３／Hrで、濾過運転開始から逆圧洗浄までの合計の散気停止時間は１０分間であった。散気停止中における引き抜きライン３２、３３からの懸濁成分の抜き取りは、運転サイクル１回ごとに１回の割合で逆圧洗浄の開始直前に行った。１回の抜き取りに要した時間は約１０秒間であった。懸濁成分の抜き取り終了後、直ちに逆圧洗浄を開始した。 The filtration time was 15 minutes, and the back pressure washing was performed for 1 minute with a sodium hypochlorite aqueous solution with an effective chlorine concentration of 5 mg / L. The aeration was 4 m 3 / Hr, and the total aeration time from the start of the filtration operation to the back pressure washing was 10 minutes. The suspension components were extracted from the drawing lines 32 and 33 during the stop of the aeration immediately before the start of the back pressure washing at a rate of once per operation cycle. The time required for one extraction was about 10 seconds. Immediately after the suspension component was removed, back pressure washing was started.

実施例３の濾過運転開始時の透水速度は０．８ｍ／日であり、３ヶ月経過後の透水速度は０．７ｍ／日であった。このように短時間で効率よくスラッジを抜き取ることができるため、長期間、安定した濾過運転をすることができた。   The water transmission rate at the start of the filtration operation in Example 3 was 0.8 m / day, and the water transmission rate after 3 months was 0.7 m / day. Since sludge can be efficiently extracted in a short time as described above, a stable filtration operation can be performed for a long time.

実施例４
（ｄ）の処理法を適用し、実施例１と同様にして、図２に示す運転条件にて濾過運転を行った（ＯＮは散気中、ＯＦＦは散気停止）。 Example 4
The treatment method (d) was applied, and the filtration operation was performed under the operation conditions shown in FIG. 2 in the same manner as in Example 1 (ON is aeration, OFF is aeration stop).

濾過時間は15分、逆圧洗浄は、有効塩素濃度5mg/Lによる次亜塩素酸ナトリウム水溶液による逆洗を１分間行った。散気は４m３／Hrで、逆圧洗浄の開始直後（約１０秒間）にのみ停止した。散気停止中における引き抜きライン３２、３３から懸濁成分を抜き取りは、運転サイクル１回ごとに１回の割合で逆圧洗浄の開始直後に行った。１回の抜き取りに要した時間は約１０秒間であった。 The filtration time was 15 minutes, and the back pressure washing was performed for 1 minute with a sodium hypochlorite aqueous solution with an effective chlorine concentration of 5 mg / L. The aeration was 4 m 3 / Hr and stopped only immediately after the start of backwashing (about 10 seconds). The suspended components were extracted from the drawing lines 32 and 33 during the stop of the aeration immediately after the start of the back pressure washing at a rate of once per operation cycle. The time required for one extraction was about 10 seconds.

実施例４の濾過運転開始時の透水速度は０．８ｍ／日であり、３ヶ月経過後の透水速度は０．７ｍ／日であった。このように短時間で効率よくスラッジを抜き取ることができるため、長期間、安定した濾過運転をすることができた。   The water transmission rate at the start of the filtration operation in Example 4 was 0.8 m / day, and the water transmission rate after 3 months was 0.7 m / day. Since sludge can be efficiently extracted in a short time as described above, a stable filtration operation can be performed for a long time.

本発明の排水処理方法で用いる水処理装置の概略断面図。The schematic sectional drawing of the water treatment apparatus used with the waste water treatment method of this invention. 実施例の運転条件を説明するための概念図。The conceptual diagram for demonstrating the driving | running condition of an Example.

符号の説明Explanation of symbols

１０ 排水水処理装置
１１ 処理槽
１２ 外圧型濾過膜
１３ 仕切板
１４ 凝集反応槽
１５ 濾過槽
２０ 凝集剤投入装置
DESCRIPTION OF SYMBOLS 10 Waste water treatment apparatus 11 Treatment tank 12 External pressure type filtration membrane 13 Partition plate 14 Aggregation reaction tank 15 Filtration tank 20 Coagulant input device

Claims (4)

濾過膜及び散気管を備えた処理槽と、前記処理槽に凝集剤を投入する凝集剤投入手段を有する排水処理装置を用い、凝集、濾過及び逆圧洗浄をする排水処理方法であり、
前記濾過膜による濾過運転中又は逆圧洗浄中に前記散気管からの散気を停止した後、前記処理槽の下部から懸濁成分を除去する排水処理方法。 A wastewater treatment method using a wastewater treatment apparatus having a treatment tank equipped with a filtration membrane and an air diffuser and a flocculant charging means for charging a flocculant into the treatment tank, and performing agglomeration, filtration and back pressure washing,
A wastewater treatment method for removing suspended components from the lower part of the treatment tank after stopping the aeration from the aeration tube during the filtration operation by the filtration membrane or during the reverse pressure washing. 懸濁成分の除去を、散気の開始前又は開始後に行う、請求項１記載の排水処理方法。   The wastewater treatment method according to claim 1, wherein the suspension component is removed before or after the start of the aeration. 前記濾過膜による濾過運転を停止して前記濾過膜の逆圧洗浄をするとき、逆圧洗浄開始前の濾過運転中に、前記処理槽の下部から懸濁成分を除去する請求項１又は２記載の排水処理方法。   The suspension component is removed from the lower part of the treatment tank during the filtration operation before the start of the reverse pressure washing when the filtration operation by the filtration membrane is stopped and the filtration membrane is back pressure washed. Wastewater treatment method. 前記濾過膜による濾過運転を停止して前記濾過膜の逆圧洗浄をするとき、逆圧洗浄開始後の逆圧洗浄中に、前記処理槽の下部から懸濁成分を除去する請求項１又は２記載の排水処理方法。


The suspension component is removed from the lower part of the treatment tank during back pressure cleaning after the start of back pressure cleaning when the filtration operation by the filter membrane is stopped and back pressure cleaning of the filter membrane is performed. The described waste water treatment method.


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JP7299022B2 (en) 2015-11-27 2023-06-27 ケミラ ユルキネン オサケイティエ Improving Phosphorus Deposition and Membrane Flux in Membrane Bioreactors

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