JP2005144291A - Method for controlling aeration quantity - Google Patents

Method for controlling aeration quantity Download PDF

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JP2005144291A
JP2005144291A JP2003383781A JP2003383781A JP2005144291A JP 2005144291 A JP2005144291 A JP 2005144291A JP 2003383781 A JP2003383781 A JP 2003383781A JP 2003383781 A JP2003383781 A JP 2003383781A JP 2005144291 A JP2005144291 A JP 2005144291A
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membrane
differential pressure
aeration
air volume
membrane separation
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Motoharu Noguchi
基治 野口
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NGK Insulators Ltd
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for controlling aeration quantity capable of reducing an energy cost by suppressing the aeration quantity up to the minimum level low and responding to the usual change of filtration conditions. <P>SOLUTION: Inside a treating tank 2 such as a biological reactor in an activated sludge method, a membrane separator 3 in which a membrane filtration module comprising a filter membrane for separating raw water (a) to be treated into a sludge solid component and treated water (b) is loaded is immersed and disposed and, just under the membrane separator, an aerator 4 is attached and diffuses the air supplied from a blower 41 and floated air bubbles wash the membrane separator 3. A membrane differential pressure of the membrane separator 3 is monitored by a pressure sensor 32 and, at the non-stationary time when the membrane differential pressure rises suddenly over the predetermined value, the aeration quantity supplied from the aerator 4 is increased. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

本発明は、膜分離活性汚泥法における曝気風量の制御方法の改良に関する。   The present invention relates to an improvement in a method for controlling the amount of aeration air in a membrane separation activated sludge method.

従来、汚泥など汚濁固形分を含む汚水を固液分離する膜分離装置は、特許文献１〜６にあるように実用化されている。その基本的構造について図２によって概説すると、この膜分離装置１１には、汚水を汚濁固形分と処理水とに分離するためのろ過膜からなる膜ろ過モジュールが格納されていて、例えば活性汚泥法における生物反応槽などの処理槽１の内部に浸漬、配設される。そして、その直下には曝気装置１２が付設され、ブロア１３から送給される空気を散気して、浮上した気泡が膜分離装置１１に沿って上昇するように構成されている。
特開平９−１３６０２１号公報：解決手段、図。 特開平１０−３４１８１号公報：解決手段、図。 特開平１０−２９６２５２号公報：解決手段、図。 特開２００２−１６６２７６号公報：解決手段、図。 特開２００２−２１０４８６号公報：解決手段、図。 特開２００２−２９２２５４号公報：解決手段、図。 Conventionally, a membrane separation apparatus for solid-liquid separation of sewage containing contaminated solids such as sludge has been put into practical use as disclosed in Patent Documents 1-6. The basic structure will be outlined with reference to FIG. 2. The membrane separation device 11 stores a membrane filtration module comprising a filtration membrane for separating sewage into polluted solids and treated water. Is immersed and disposed in a processing tank 1 such as a biological reaction tank. An aeration device 12 is attached immediately below, and is configured so that air supplied from the blower 13 is diffused so that the air bubbles that have risen rise along the membrane separation device 11.
Japanese Patent Laid-Open No. 9-136021: Solution means, diagram. Japanese Patent Laid-Open No. 10-34181: Solution means, diagram. Japanese Patent Laid-Open No. 10-296252: Solution means, diagram. Unexamined-Japanese-Patent No. 2002-166276: Solution means, figure. Unexamined-Japanese-Patent No. 2002-210486: Solution means, figure. Unexamined-Japanese-Patent No. 2002-292254: Solution means, figure.

かくして、処理槽１に導入された汚泥など汚濁固形分を含む汚水である処理原水ａは、膜分離装置１１によって固液分離され、固形分を除いた処理水ｂは、排水ポンプ１４によって排出される。なお、処理水ｂは、排水ポンプ１４を用いずに水位差を駆動力とした方法でも良い。この場合、膜分離装置１１に沿って上昇する気泡は、その上昇流によってろ過膜面に付着する固形分を除去し、また付着するのを抑制するなどして、目詰まりによるろ過抵抗の増加を抑えるよう作用するのである。   Thus, the treated raw water a, which is sewage containing contaminated solids such as sludge introduced into the treatment tank 1, is solid-liquid separated by the membrane separator 11, and the treated water b excluding the solids is discharged by the drainage pump 14. The The treated water b may be a method using the water level difference as a driving force without using the drain pump 14. In this case, the bubbles rising along the membrane separation device 11 remove the solid content adhering to the filtration membrane surface by the upward flow and suppress the adhesion, thereby increasing the filtration resistance due to clogging. It acts to suppress it.

このように、膜分離装置１１に対する曝気運転は、膜分離装置１１の運転に対応して常時運転され、かつかなりの曝気風量を確保する必要があることから、ブロア１３を運転するためのエネルギコストは、通常、処理槽１基当たりの全ランニングコストの１８〜３７％を占めるなど、そのウエイトがかなり高いという実情があった。   As described above, since the aeration operation for the membrane separation device 11 is always operated corresponding to the operation of the membrane separation device 11 and it is necessary to secure a considerable amount of aeration air, the energy cost for operating the blower 13 is required. Usually accounted for 18 to 37% of the total running cost per treatment tank, and the weight was considerably high.

一方、エネルギコスト節減のため曝気風量のレベルを単純に低下させると、処理原水の汚濁物濃度や流量の日常変動、あるいは生物反応条件の変化、その他ろ過条件の変動などがあったとき、膜差圧が急上昇し対応できないという問題があった。   On the other hand, if the level of aeration air volume is simply reduced to save energy costs, there will be membrane differences when there are daily fluctuations in the concentration and flow rate of raw water in the treated raw water, changes in biological reaction conditions, fluctuations in other filtration conditions, etc. There was a problem that the pressure rose rapidly and could not be dealt with.

本発明は、上記の問題点を解決するためになされたものであり、曝気風量を最低のレベルを低く抑えることによりエネルギコストを抑制するとともに、日常のろ過条件の変動にも対応することを可能とする曝気風量の制御方法を提供する。   The present invention has been made in order to solve the above-described problems, and by suppressing the aeration air volume to a minimum level, it is possible to suppress energy costs and cope with fluctuations in daily filtration conditions. A method for controlling the amount of aeration air is provided.

上記の問題は、生物処理槽内に配設した、曝気装置を付設した膜分離装置を用いる膜分離活性汚泥法において、前記膜分離装置の膜差圧を監視し、膜差圧が所定値以上に急上昇する非定常時には、前記曝気装置から供給される曝気風量を増加させるよう制御することを特徴とする本発明の曝気風量の制御方法によって、解決することができる。ここで膜差圧が所定値以上に急上昇したか否かは、膜差圧上昇速度（例えばｋＰａ／日で表す）で評価される。また、膜差圧は水温の影響を受けるため、処理槽内の水温を測定し、水温補正した値を用いる方が望ましい。
また、本発明は、膜差圧が非定常時を除く通常のレベルの範囲内であるときの曝気風量を、あらかじめ定めた許容下限値に設定する形態の曝気風量の制御方法として具体化される。 In the membrane separation activated sludge method using a membrane separation device provided with an aeration device, disposed in a biological treatment tank, the membrane differential pressure of the membrane separation device is monitored, and the membrane differential pressure exceeds a predetermined value. In a non-stationary state where the aeration suddenly increases, the aeration air volume control method according to the present invention can be solved by controlling to increase the aeration air volume supplied from the aeration apparatus. Here, whether or not the membrane differential pressure has rapidly increased to a predetermined value or more is evaluated by a membrane differential pressure increase rate (for example, expressed in kPa / day). Further, since the membrane differential pressure is affected by the water temperature, it is desirable to measure the water temperature in the treatment tank and use a value obtained by correcting the water temperature.
In addition, the present invention is embodied as a method for controlling the aeration air volume in such a manner that the aeration air volume when the membrane differential pressure is within a normal level range excluding unsteady times is set to a predetermined allowable lower limit value. .

本発明者らは、生物処理槽内に配設した、曝気装置を付設した膜分離装置を用いる膜分離活性汚泥法における、曝気風量と膜分離装置の目詰まり防止作用の関係や、処理槽のろ過条件の変動要因、例えば前記したような処理原水の汚濁物濃度や流量の日常変動、あるいは生物反応条件の変化、その他ろ過条件について、多くの実機を研究、調査した結果、次の（１）（２）の事実を見出したことから本発明を完成したのである。   In the membrane separation activated sludge method using a membrane separation device provided with an aeration device, disposed in a biological treatment tank, the relationship between the amount of aeration air and the clogging prevention effect of the membrane separation device, As a result of researching and investigating many factors related to fluctuation conditions of filtration conditions, such as daily fluctuations in the concentration and flow rate of treated raw water, changes in biological reaction conditions, and other filtration conditions, the following (1) The present invention was completed from finding the fact (2).

（１）膜分離装置のろ過抵抗に急激に悪影響を及ぼすろ過条件は、日常変動の大部分を占める緩慢な変動ではなく、短時間の相当に急激な変動であって、そのような非定常的な変動は、膜分離装置の膜差圧の動きを常時監視していて、それが所定値以上に急上昇した場合に発生したと判断することができることを見出した。   (1) Filtration conditions that have a detrimental effect on the filtration resistance of the membrane separation apparatus are not slow fluctuations that account for the majority of daily fluctuations, but rather abrupt fluctuations in a short period of time. It has been found that such a fluctuation can be judged to occur when the movement of the membrane differential pressure of the membrane separation apparatus is constantly monitored and when it rapidly rises above a predetermined value.

（２）定常的なろ過条件では、膜分離装置のろ過抵抗は緩慢に増加するものであって、これは曝気風量を増加させても抑止効果は比例的に増加しないが、また曝気風量を順次低下させた場合、ある値以下に下がるとろ過抵抗は急激に増加することを見出した。すなわち、定常的なろ過条件では、前記のようなろ過抵抗が急激に増加する現象がおきる直前の曝気風量を許容下限値としてろ過運転するのが、ろ過抵抗の増加を極力抑制し、かつ曝気風量を最小にできることが分かったのである。   (2) Under steady filtration conditions, the filtration resistance of the membrane separator increases slowly, and this does not increase the suppression effect proportionally even if the aeration air volume is increased. It was found that the filtration resistance suddenly increases when the value drops below a certain value. In other words, under steady filtration conditions, the filtration operation is performed with the aeration air volume immediately before the phenomenon of the sudden increase in filtration resistance as described above being the allowable lower limit, and the increase in filtration resistance is suppressed as much as possible and the aeration air volume is It has been found that can be minimized.

かくして、本発明はこのような知見に基づいて完成したものであり、前記膜分離装置の膜差圧を監視し、膜差圧が所定値以上に急上昇する非定常時には、前記曝気装置から供給される曝気風量を増加させるよう制御するので、定常的なろ過条件では、曝気風量をミニマムに設定できるので、曝気装置のエネルギコストを抑制できる。そして、膜分離装置の目詰まりを急激に惹起するようなろ過条件の大きな変動があった場合には、曝気風量を増加させて目詰まりを抑制できるという優れた効果がある。よって本発明は、従来の問題点を解消した曝気風量の制御方法として、実用的価値はきわめて大なるものがある。   Thus, the present invention has been completed based on such knowledge. The membrane differential pressure of the membrane separation device is monitored, and the membrane differential pressure is supplied from the aeration device at a non-steady time when the membrane differential pressure rapidly rises above a predetermined value. Since the aeration air volume is controlled to be increased, the aeration air volume can be set to a minimum under a steady filtration condition, so that the energy cost of the aeration apparatus can be suppressed. When there is a large change in the filtration conditions that causes the clogging of the membrane separation device suddenly, there is an excellent effect that the clogging can be suppressed by increasing the aeration air volume. Therefore, the present invention has an extremely large practical value as a method for controlling the amount of aeration air that has solved the conventional problems.

次に、本発明の曝気風量の制御方法に係る実施形態について、図１を参照しながら説明する。
本発明が実施できる膜分離活性汚泥装置のフローを例示する図１において、その基本的な構造は先に説明したものと同様である。すなわち、例えば活性汚泥法における生物反応槽などの処理槽２の内部に、処理原水ａを汚濁固形分と処理水ｂとに分離するためのろ過膜からなる膜ろ過モジュールが格納されている膜分離装置３が、浸漬、配設される。そして、その直下には曝気装置４が付設され、ブロア４１から送給される空気を散気して、浮上した気泡が膜分離装置３に沿って上昇して洗浄するように構成されている。 Next, an embodiment according to the method for controlling the aeration air volume of the present invention will be described with reference to FIG.
In FIG. 1 illustrating the flow of the membrane separation activated sludge apparatus in which the present invention can be implemented, the basic structure is the same as that described above. That is, for example, a membrane separation module in which a membrane filtration module comprising a filtration membrane for separating the treated raw water a into contaminated solids and treated water b is stored inside the treatment tank 2 such as a biological reaction tank in the activated sludge method. A device 3 is immersed and arranged. An aeration device 4 is attached immediately below, and the air supplied from the blower 41 is diffused so that the air bubbles that have risen rise along the membrane separation device 3 and are washed.

かくして、処理槽２に導入された処理原水ａは、膜分離装置３によって固液分離され、固形分を除いた処理水ｂは、排水ポンプ３１によって排出される。この場合、膜分離装置３に沿って上昇する気泡は、その上昇流によってろ過膜面に付着する固形分を除去し、また付着するのを抑制するなどして、目詰まりによるろ過抵抗の増加を抑えるよう作用するのは如上の通りである。   Thus, the treated raw water a introduced into the treatment tank 2 is subjected to solid-liquid separation by the membrane separation device 3, and the treated water b excluding the solid content is discharged by the drainage pump 31. In this case, the bubbles rising along the membrane separation device 3 remove the solid content adhering to the filtration membrane surface by the upward flow and suppress the adhesion, thereby increasing the filtration resistance due to clogging. It is as above that it acts to suppress.

本発明は、このようなシステムを前提として、前記膜分離装置３の膜差圧を監視し、膜差圧が所定値以上に急上昇する非定常時には、前記曝気装置４から供給される曝気風量を増加させるよう制御する点を特徴とする曝気風量の制御方法であるが、この膜分離装置の運転に関して、日常のろ過条件の変動からみて、短時間ではあるが急激に変動する非定常時と、それ以外の多くの時間を占める緩慢に変動する定常時とに区分されること、およびこの非定常時と定常時の区別は、前記曝気装置４の膜差圧を常時測定することによって判断できることは、先に述べた通りである。   Based on such a system, the present invention monitors the membrane differential pressure of the membrane separation device 3 and determines the amount of aeration air supplied from the aeration device 4 when the membrane differential pressure suddenly rises above a predetermined value. Although it is a control method of the aeration air volume characterized by controlling to increase, regarding the operation of this membrane separation device, from the fluctuation of daily filtration conditions, it is a short-time but abrupt fluctuation, It can be determined by constantly measuring the membrane differential pressure of the aeration apparatus 4 that it is divided into the steady state that slowly changes and occupies many other times, and the distinction between the unsteady time and the steady time. As described above.

そこで、本発明においては、膜差圧の挙動が定常時のレベルにあるときの曝気風量として、これ以下に低下させると膜差圧が急激に増加するという許容される下限の曝気風量（許容下限値）をあらかじめ予備試験によって定めておき、その許容下限値に設定するのが好ましい。なお、この許容下限値は、個々のシステムや処理原水水質などによってその値が変化するので一概に定めることができないが、このように、低常時の曝気風量を許容下限値としてろ過運転すれば、ろ過抵抗の増加を極力抑制し、かつ曝気風量を最小にできるのである。   Therefore, in the present invention, as the aeration air volume when the behavior of the membrane differential pressure is at a steady level, the lower limit aeration air volume (allowable lower limit) that the membrane differential pressure rapidly increases when the behavior is reduced below this level. (Value) is preferably determined in advance by a preliminary test and set to the allowable lower limit value. Note that this allowable lower limit value cannot be determined unconditionally because the value varies depending on the individual system and the quality of the treated raw water, etc.In this way, if filtration operation is carried out with the low normal aeration air volume as the allowable lower limit value, The increase in filtration resistance can be suppressed as much as possible and the aeration air volume can be minimized.

そして、本発明では、圧力センサ３２を前記膜分離装置３のろ過側に設置し、ろ過膜の膜差圧を常時監視するものとし、膜差圧が所定値以上に急上昇する非定常時には、前記曝気装置４から供給される曝気風量を増加させ、分離膜面に対する汚濁固形分の付着や堆積を防止、解消するよう制御する点を最大の特徴とする。なお、膜差圧は、膜を通して処理水を得る際に膜の原水側と透過側（処理水側）で生じる圧力の差のことである。   And in this invention, the pressure sensor 32 shall be installed in the filtration side of the said membrane separator 3, and the membrane differential pressure | voltage of a filtration membrane shall always be monitored, and at the time of the unsteady state where a membrane differential pressure | voltage rises more than a predetermined value, The greatest feature is that the amount of aeration air supplied from the aeration device 4 is increased, and control is performed so as to prevent and eliminate adhesion and accumulation of contaminated solids on the separation membrane surface. The membrane differential pressure is a difference in pressure generated between the raw water side and the permeate side (treated water side) of the membrane when the treated water is obtained through the membrane.

さらに、この非定常時が生じたことを判断するための膜差圧の所定値および急上昇の程度は、個々のシステムについて実験的に定められるが、多くの経験からその膜差圧の所定値は、０〜１５０ｋＰａの範囲内、好ましくは０〜２０ｋＰａの範囲内で設定するのがよく、また、膜差圧の急上昇の程度は、１ｋＰａ／日以上が１時間以上継続する場合に設定するのが好ましい。   Further, the predetermined value of the membrane differential pressure and the degree of sudden rise for determining that this unsteady time has occurred are experimentally determined for each system, but from many experiences, the predetermined value of the membrane differential pressure is In the range of 0 to 150 kPa, preferably in the range of 0 to 20 kPa, the degree of rapid increase in the membrane differential pressure is set when 1 kPa / day or more continues for 1 hour or more. preferable.

かくして、本発明では、定常的なろ過条件では、曝気風量をミニマムに設定できるので、曝気装置のエネルギコストを抑制でき、平均的な処理槽１基当たりエネルギコストを最大６０％程度節減することができた。そして、膜分離装置の目詰まりを急激に惹起するようなろ過条件の大きな変動があった場合には、曝気風量を増加させて目詰まりを抑制できるという優れた効果がある。よって本発明は、従来の問題点を解消した曝気風量の制御方法として、実用的価値はきわめて大なるものがある。   Thus, in the present invention, since the aeration air volume can be set to a minimum under the steady filtration conditions, the energy cost of the aeration apparatus can be suppressed, and the average energy cost per treatment tank can be reduced by about 60%. did it. When there is a large change in the filtration conditions that causes the clogging of the membrane separation device suddenly, there is an excellent effect that the clogging can be suppressed by increasing the aeration air volume. Therefore, the present invention has an extremely large practical value as a method for controlling the amount of aeration air that has solved the conventional problems.

なお、本発明が適用される処理槽としては、通常の生物反応槽を含み、下水、返流水、工場排水、ゴミ浸出水、し尿廃水、農業廃水、畜産廃水、養殖廃水など広範囲の処理原水の排水処理に利用されている活性汚泥を用いる生物処理槽の他、一般的な好気槽、硝化液循環法による硝化＋脱窒処理槽、ＡＯ法またはＡ２Ｏ法などによる処理槽やこれらに微生物固定化担体を組み合わせた処理槽を含むのである。また、これらの処理槽の後に生物処理槽とは別に膜分離槽を設けてもよい。   The treatment tank to which the present invention is applied includes a normal biological reaction tank, and includes a wide range of raw water for treatment such as sewage, return water, industrial wastewater, waste leachate, human waste wastewater, agricultural wastewater, livestock wastewater, and aquaculture wastewater. In addition to biological treatment tanks using activated sludge used for wastewater treatment, general aerobic tanks, nitrification and denitrification treatment tanks by nitrification liquid circulation method, treatment tanks by AO method or A2O method, etc. It includes a treatment tank combined with a chemical carrier. Moreover, you may provide a membrane separation tank separately from a biological treatment tank after these treatment tanks.

また、本発明の適用され得る膜分離装置としては、外圧方式または内圧方式のいずれでもよく、使用される膜は、高分子材（ＰＥＧ、ＰＶＡ、ＰＰ、ＰＵ、ＰＥ、ＰＶｄＦなど合成樹脂材料）またはセラミックス材料を用いたＭＦ膜およびＵＦ膜であり、そのろ過体形状は、モノリス、チューブラー、ハニカム、中空糸、または平膜状などの多くの形式の膜分離装置に適用される。   The membrane separation apparatus to which the present invention can be applied may be either an external pressure method or an internal pressure method, and the membrane used is a polymer material (synthetic resin material such as PEG, PVA, PP, PU, PE, PVdF). Or it is the MF membrane and UF membrane using ceramic material, The filter body shape is applied to many types of membrane separators, such as monolith, tubular, honeycomb, hollow fiber, or flat membrane shape.

本発明を説明するための膜分離活性汚泥装置のフロー概要図。The flow schematic diagram of the membrane separation activated sludge apparatus for demonstrating this invention. 従来の膜分離活性汚泥装置のフロー概要図。The flow schematic diagram of the conventional membrane separation activated sludge apparatus.

符号の説明Explanation of symbols

２：処理槽
３：膜分離装置、３１：排水ポンプ、３２：圧力センサ
４：曝気装置
ａ：処理原水
ｂ：処理水

2: treatment tank 3: membrane separation device, 31: drainage pump, 32: pressure sensor 4: aeration device a: treated raw water b: treated water

Claims (2)

生物処理槽内に配設した、曝気装置を付設した膜分離装置を用いる膜分離活性汚泥法において、前記膜分離装置の膜差圧を監視し、膜差圧が所定値以上に急上昇する非定常時には、前記曝気装置から供給される曝気風量を増加させるよう制御することを特徴とする曝気風量の制御方法。   In a membrane separation activated sludge method using a membrane separation device provided with an aeration device disposed in a biological treatment tank, the membrane differential pressure of the membrane separation device is monitored, and the membrane differential pressure rapidly rises above a predetermined value A control method of the aeration air volume, characterized in that control is performed to increase the aeration air volume supplied from the aeration apparatus. 膜差圧が非定常時を除く通常のレベルの範囲内であるときの曝気風量を、あらかじめ定めた許容定常値に設定する請求項１に記載の曝気風量の制御方法。

The aeration air volume control method according to claim 1, wherein the aeration air volume when the membrane differential pressure is within a normal level range excluding unsteady time is set to a predetermined allowable steady value.

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