JP2012206040A - Treatment method and treatment apparatus of organic matter containing wastewater - Google Patents
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- 239000005416 organic matter Substances 0.000 title claims abstract description 35
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/006—Regulation methods for biological treatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
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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
- Y02W10/20—Sludge processing
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Abstract
Description
本発明は有機物含有排水を嫌気性生物処理した後好気性生物処理し、好気性生物処理水を膜分離処理する有機物含有排水の処理方法及び処理装置に係り、特に、嫌気性生物処理槽の後の好気性生物処理槽として、膜分離活性汚泥式の好気性生物処理槽を採用した有機物含有排水の処理において、好気性生物処理汚泥の膜濾過性を改善して膜の透過水量（フラックス）を高く維持し、また薬品洗浄頻度を低減する有機物含有排水の処理方法及び処理装置に関する。 The present invention relates to an organic matter-containing wastewater treatment method and treatment apparatus in which an organic matter-containing wastewater is subjected to anaerobic biological treatment followed by aerobic biological treatment, and the aerobic biological treatment water is subjected to membrane separation treatment. As an aerobic biological treatment tank, a membrane-separated activated sludge type aerobic biological treatment tank adopts organic matter-containing wastewater, improves the membrane filterability of the aerobic biological treatment sludge and reduces the amount of permeated water (flux) of the membrane. The present invention relates to a method and apparatus for treating wastewater containing organic matter that is kept high and reduces the frequency of chemical cleaning.
従来、有機物含有排水の処理方法として、有機物含有排水を嫌気性生物処理した後、好気性生物処理し、好気性生物処理水を固液分離する方法が知られている（例えば特許文献１）。
また、好気性生物処理水の固液分離手段として、膜分離装置を用いて活性汚泥を濃縮する膜分離活性汚泥法も知られている（例えば特許文献２）。
Conventionally, as a method for treating organic matter-containing wastewater, a method is known in which an organic matter-containing wastewater is subjected to anaerobic biological treatment, followed by aerobic biological treatment, and aerobic biologically treated water is solid-liquid separated (for example, Patent Document 1).
As a solid-liquid separation means for aerobic biologically treated water, a membrane separation activated sludge method is also known in which activated sludge is concentrated using a membrane separation device (for example, Patent Document 2).
好気性生物処理水の固液分離手段として膜分離装置を用いる場合、嫌気性生物処理は、膜汚泥の原因となる代謝産物の生成量が、好気性生物処理よりも少ないため、有機物含有排水（原水）を直接好気性生物処理した後膜分離処理する場合よりも、好気性生物処理の前段に嫌気性生物処理を行う場合の方が、膜汚染が低減され、膜の薬品洗浄頻度を少なくすることができるという利点がある。 In the case of using a membrane separation device as a solid-liquid separation means for aerobic biologically treated water, anaerobic biological treatment produces less amount of metabolites that cause membrane sludge than aerobic biological treatment. When the anaerobic biological treatment is performed before the aerobic biological treatment, the membrane contamination is reduced and the chemical cleaning frequency of the membrane is reduced compared to the case where the raw water is directly subjected to the aerobic biological treatment and then the membrane separation treatment. There is an advantage that you can.
前述の如く、好気性生物処理水を膜分離装置で固液分離する場合、好気性生物処理の前段で嫌気性生物処理を行うことにより、代謝産物による膜汚染を低減することができるが、嫌気性生物処理では、好気性生物処理に比べて、粘質物の生成量が少なく、フロックの形成力が弱いため、直径１０μｍ未満の微細なＳＳ成分が嫌気性生物処理水に含まれるようになる。これら微細なＳＳ成分は、後段の好気処理の後にも多くが残留し、膜分離処理において、膜表面に緻密なケーク層を形成し、膜間差圧を上昇させやすい。このため、嫌気性生物処理水を好気性生物処理し、膜分離装置で固液分離を行って、ＳＳ成分のない清澄な処理水を得ようとした場合には、膜フラックスを高く取れない；膜の薬品洗浄を頻繁に行う必要がある；といった問題があった。 As described above, when aerobic biological treatment water is solid-liquid separated with a membrane separation device, anaerobic biological treatment can be performed before the aerobic biological treatment to reduce membrane contamination by metabolites. Compared to the aerobic biological treatment, the anaerobic biological treatment water contains a fine SS component having a diameter of less than 10 μm because the amount of mucilage produced is small and the floc forming ability is weak compared to the aerobic biological treatment. Many of these fine SS components remain after the subsequent aerobic treatment, and in the membrane separation treatment, a dense cake layer is formed on the membrane surface, and the transmembrane pressure difference is likely to increase. For this reason, when anaerobic biological treatment water is subjected to aerobic biological treatment and solid-liquid separation is performed with a membrane separation device to obtain a clear treated water having no SS component, a high membrane flux cannot be obtained; There is a problem that chemical cleaning of the membrane needs to be performed frequently.
本発明は上記従来の問題点を解決し、有機物含有排水を嫌気性生物処理した後好気性生物処理し、好気性生物処理水を膜分離処理するに当たり、好気性生物処理汚泥の膜濾過性を改善して膜フラックスを高く維持して、膜の薬品洗浄頻度を低減する有機物含有排水の処理方法及び有機物含有排水の処理装置を提供することを課題とする。 The present invention solves the above-mentioned conventional problems, anaerobic biological treatment of wastewater containing organic matter, followed by aerobic biological treatment, the membrane filterability of the aerobic biological treatment sludge in the membrane separation treatment It is an object of the present invention to provide an organic matter-containing wastewater treatment method and an organic matter-containing wastewater treatment apparatus that improve and maintain a high membrane flux and reduce the frequency of chemical cleaning of the membrane.
本発明者は、上記課題を解決すべく鋭意検討した結果、膜分離活性汚泥式の好気性生物処理槽における汚泥滞留時間を制御することにより、好気性生物処理槽内での微細ＳＳ成分の分解が促進されることで、好気性生物処理汚泥の膜濾過性が改善され、後段の膜分離装置の膜フラックスが向上することを見出した。 As a result of intensive studies to solve the above-mentioned problems, the present inventor has decomposed the fine SS component in the aerobic biological treatment tank by controlling the sludge residence time in the membrane separation activated sludge type aerobic biological treatment tank. As a result, it was found that the membrane filterability of the aerobic biologically treated sludge was improved, and the membrane flux of the subsequent membrane separator was improved.
本発明はこのような知見に基いて達成されたものであり、以下を要旨とする。 The present invention has been achieved on the basis of such findings, and the gist thereof is as follows.
［１］ 有機物含有排水を嫌気的に生物処理する嫌気性生物処理工程と、該嫌気性生物処理工程から流出する嫌気性生物処理水を好気的に生物処理する好気性生物処理工程と、該好気性生物処理工程の好気性生物処理水を固液分離する膜分離工程とを有する有機物含有排水の処理方法において、該好気性生物処理工程内における汚泥滞留時間を１５日以上に制御することを特徴とする有機物含有排水の処理方法。 [1] An anaerobic biological treatment process for anaerobically biologically treating wastewater containing organic matter, an aerobic biological treatment process for aerobically biologically treating anaerobic biological treated water flowing out of the anaerobic biological treatment process, In the method for treating organic matter-containing wastewater having a membrane separation step for solid-liquid separation of the aerobic biological treatment water in the aerobic biological treatment step, the sludge residence time in the aerobic biological treatment step is controlled to 15 days or more. A method for treating wastewater containing organic substances.
［２］ ［１］において、前記好気性生物処理工程における汚泥滞留時間を２０〜５０日に制御することを特徴とする有機物含有排水の処理方法。 [2] In [1], the sludge residence time in the aerobic biological treatment process is controlled to 20 to 50 days, and the organic material-containing wastewater treatment method is characterized in that
［３］ 有機物含有排水を嫌気的に生物処理する嫌気性生物処理槽と、該嫌気性生物処理槽から流出する嫌気性生物処理水を好気的に生物処理する好気性生物処理槽と、該好気性生物処理槽の好気性生物処理水を固液分離する膜分離手段とを有する有機物含有排水の処理装置において、該好気性生物処理槽内における汚泥滞留時間が１５日以上に制御されることを特徴とする有機物含有排水の処理装置。 [3] An anaerobic biological treatment tank for anaerobically biologically treating organic matter-containing waste water; an aerobic biological treatment tank for aerobically biologically treating anaerobic biological treated water flowing out of the anaerobic biological treatment tank; In a treatment apparatus for organic matter-containing wastewater having a membrane separation means for solid-liquid separation of aerobic biological treatment water in an aerobic biological treatment tank, the sludge residence time in the aerobic biological treatment tank is controlled to 15 days or more. Organic wastewater treatment equipment characterized by
［４］ ［３］において、前記好気性生物処理槽における汚泥滞留時間が２０〜５０日に制御されることを特徴とする有機物含有排水の処理装置。 [4] In [3], the sludge residence time in the aerobic biological treatment tank is controlled for 20 to 50 days, the organic matter-containing wastewater treatment apparatus.
［５］ ［３］又は［４］において、前記膜分離手段は、前記好気性生物処理槽内に浸漬された浸漬型膜分離装置であり、該好気性生物処理槽は余剰汚泥の引き抜き手段と、該余剰汚泥の引き抜き手段からの余剰汚泥の引き抜き量の制御手段とを有することを特徴とする有機物含有排水の処理装置。 [5] In [3] or [4], the membrane separation means is a submerged membrane separation apparatus immersed in the aerobic biological treatment tank, and the aerobic biological treatment tank includes excess sludge drawing means. And an organic substance-containing wastewater treatment apparatus, characterized in that it has a means for controlling the amount of excess sludge extracted from the means for extracting excess sludge.
本発明によれば、好気性生物処理槽の汚泥滞留時間を１５日以上好ましくは２０〜５０日に制御することにより、嫌気性生物処理で生成し、好気性生物処理槽内に流入する微細なＳＳ成分の分解を促進し、好気性生物処理汚泥の膜濾過性を改善することができ、これを固液分離する膜分離装置の膜フラックスを高く維持して、薬品洗浄頻度を低減し、効率的な処理を行うことができる。 According to the present invention, by controlling the sludge residence time of the aerobic biological treatment tank for 15 days or more, preferably 20 to 50 days, the fine sludge produced by the anaerobic biological treatment and flowing into the aerobic biological treatment tank is obtained. It can promote the decomposition of SS components and improve the membrane filterability of aerobic biological treatment sludge, maintain the membrane flux of the membrane separation device that separates this into a solid, reduce the frequency of chemical cleaning, and improve efficiency Processing can be performed.
以下に図面を参照して本発明の有機物含有排水の処理方法及び処理装置の実施の形態を詳細に説明する。 DESCRIPTION OF EMBODIMENTS Embodiments of a method and apparatus for treating organic matter-containing wastewater according to the present invention will be described in detail below with reference to the drawings.
図１は、本発明の有機物含有排水の処理装置の実施の形態の一例を示す系統図であり、図１において、１は嫌気性生物処理槽、２は好気性生物処理槽である。嫌気性生物処理槽１内には担体３が充填されている。好気性生物処理槽２内には、浸漬型膜モジュール４が浸漬配置され、膜モジュール４の下方には散気管（曝気手段）５が設けられている。Ｐ１，Ｐ２はポンプであり、ＰＩは圧力計である。 FIG. 1 is a system diagram showing an example of an embodiment of the organic matter-containing wastewater treatment apparatus of the present invention. In FIG. 1, 1 is an anaerobic biological treatment tank, and 2 is an aerobic biological treatment tank. The anaerobic biological treatment tank 1 is filled with a carrier 3. An immersion type membrane module 4 is immersed in the aerobic biological treatment tank 2, and an aeration tube (aeration means) 5 is provided below the membrane module 4. P 1 and P 2 are pumps, and PI is a pressure gauge.
図１において、有機物含有排水（原水）は、配管１１より嫌気性生物処理槽１の底部に導入され、嫌気性生物処理槽１内を上向流で流れる間に嫌気性生物処理され、嫌気性生物処理水は配管１２より好気性生物処理槽２に導入される。好気性生物処理槽２内の好気性生物処理水は、膜モジュール４で固液分離され、膜透過水が処理水として配管１３より取り出される。余剰汚泥は配管１４より抜き出される。
In FIG. 1, organic matter-containing wastewater (raw water) is introduced into the bottom of an anaerobic biological treatment tank 1 through a
嫌気性生物処理槽１の処理方式としては特に限定されず、図１に示すような流動性担体３を充填した流動床式の他、固定床式処理槽であってもよく、また、槽内に高密度で沈降性の大きいグラニュール汚泥のスラッジブランケットを形成し、原水を上向流通液して高負荷高速処理を行うＵＡＳＢ（Upflow Anaerobic Sludge Blanket：上向流嫌気性スラッジブランケット）法や、このＵＡＳＢ法よりもさらに高さの高い反応槽を用いて高流速で原水を通液し、スラッジブランケットを高展開率で展開させてさらなる高負荷で嫌気性処理を行うＥＧＳＢ（Expanded Granule Sludge Blanket）法であってもよい。
また、酸生成反応とメタン生成反応を同一の処理槽内で行う１相式であってもよく、各反応を別の処理槽で行う２相式であってもよい。
The treatment method of the anaerobic biological treatment tank 1 is not particularly limited, and may be a fixed bed type treatment tank in addition to a fluidized bed type filled with a fluid carrier 3 as shown in FIG. A sludge blanket of granulated sludge with high density and high sedimentation, and UASB (Upflow Anaerobic Sludge Blanket) method that performs high-load high-speed treatment by upward flow of raw water, EGSB (Expanded Granule Sludge Blanket), which uses raw reaction water at a high flow rate in a reaction tank that is higher than the UASB method, and develops sludge blankets at a high expansion rate for anaerobic treatment at higher loads. It may be a law.
Moreover, the 1 phase type which performs an acid production | generation reaction and a methane production | generation reaction in the same processing tank may be sufficient, and the 2 phase type which performs each reaction in another processing tank may be sufficient.
担体を用いた流動床式処理槽、固定床式処理槽や、ＵＡＳＢ、ＥＧＳＢのようなグラニュールを用いた処理槽は、ＣＯＤＣｒ負荷５ｋｇ／ｍ３・ｄ以上の高負荷処理ができるため好ましい。 A fluidized bed type processing tank using a carrier, a fixed bed type processing tank, and a processing tank using granules such as UASB and EGSB are preferable because high load processing with a COD Cr load of 5 kg / m 3 · d or more can be performed. .
図１に示す好気性生物処理槽２は、槽内に膜モジュール４を浸漬配置した浸漬型膜分離活性汚泥処理槽であるが、膜モジュールはこのように好気性生物処理槽２内に設けるものに限らず、好気性生物処理槽２外に膜モジュールを設ける槽外型膜分離活性汚泥法を採用するものであってもよい。槽外型膜分離活性汚泥法の場合、処理槽２とは別に設けた曝気槽内に膜モジュールを浸漬して膜透過水を得、膜濃縮水を好気性生物処理槽２に循環してもよい。 The aerobic biological treatment tank 2 shown in FIG. 1 is a submerged membrane separation activated sludge treatment tank in which a membrane module 4 is immersed in the tank. The membrane module is provided in the aerobic biological treatment tank 2 in this way. Not limited to this, an outside tank type membrane separation activated sludge method in which a membrane module is provided outside the aerobic biological treatment tank 2 may be adopted. In the case of the outside membrane separation activated sludge method, the membrane module is immersed in an aeration tank provided separately from the treatment tank 2 to obtain a membrane permeate, and the membrane concentrated water is circulated to the aerobic biological treatment tank 2. Good.
浸漬型膜モジュールではなく、通常の膜モジュールを用いることも可能であるが、動力が比較的小さくて済むこと、及びせん断力が比較的かからないため汚泥の大きさが小さくならず、膜の目詰まりが生じにくいことから、浸漬型膜モジュールを採用することが好ましい。 Although it is possible to use a normal membrane module instead of a submerged membrane module, the power is relatively small and the shearing force is relatively low, so the size of the sludge is not reduced and the membrane is clogged. Therefore, it is preferable to employ a submerged membrane module.
膜の種類としては、ＳＳの固液分離性に優れたＭＦ（精密濾過）膜やＵＦ（限外濾過）膜を用いることができ、その型式としては特に制限はなく、平膜、チューブラ膜、中空糸膜のいずれも採用することができる。 As the type of membrane, an MF (microfiltration) membrane or a UF (ultrafiltration) membrane excellent in solid-liquid separation of SS can be used, and there is no particular limitation on the type thereof, a flat membrane, a tubular membrane, Any of the hollow fiber membranes can be employed.
図１の好気性生物処理槽２では、膜モジュール４の下方に散気管５が設けられているが、このように膜モジュール４の下方に散気管５を設けることにより、膜モジュール４の膜面付着物が散気による曝気流の洗浄作用で一部剥離除去され、膜透過性が高められる。
In the aerobic biological treatment tank 2 of FIG. 1, the
なお、好気性生物処理槽２は多段に設け、例えば、前段を脱窒槽とし、後段を硝化槽として、硝化槽から脱窒槽に汚泥を循環させるようにしてもよい。この場合、膜モジュールは硝化槽又は硝化槽の汚泥を循環させる別の曝気槽（膜浸漬槽）に設けることが好ましい。 The aerobic biological treatment tank 2 may be provided in multiple stages. For example, the first stage may be a denitrification tank and the latter stage may be a nitrification tank, and sludge may be circulated from the nitrification tank to the denitrification tank. In this case, the membrane module is preferably provided in the nitrification tank or another aeration tank (membrane immersion tank) that circulates the sludge in the nitrification tank.
本発明において、このような有機物含有排水の処理において、好気性生物処理槽２の汚泥滞留時間（ＳＲＴ）を１５日以上、好ましくは２０〜５０日に制御する。具体的には、好気性生物処理槽２の汚泥滞留時間が１５日以上、好ましくは２０〜５０日となるように、配管１４からの余剰汚泥の引き抜き量を制御する。好気性生物処理槽２における汚泥滞留時間を１５日以上、好ましくは２０日以上とすることにより、嫌気性生物処理槽１で生成し、好気性生物処理槽２に流入した微細なＳＳ成分の分解を促進し、好気性生物処理汚泥の膜濾過性を改善し、膜フラックスの低下を防止することができる。ただし、好気性生物処理槽２の汚泥滞留時間を過度に長くしても、それに見合う効果は得られず、汚泥滞留時間を長くするための好気性生物処理槽容量が過大になり、また、汚泥の自己消化産物が増加し、膜を汚染しやすくなることから、好気性生物処理槽２の汚泥滞留時間は５０日以下、特に３０日以下とすることが好ましい。
In the present invention, the sludge residence time (SRT) of the aerobic biological treatment tank 2 is controlled to 15 days or more, preferably 20 to 50 days, in the treatment of such organic matter-containing wastewater. Specifically, the amount of excess sludge withdrawn from the
好気性生物処理槽２のその他の処理条件としては、ＣＯＤＣｒ負荷０．７〜５ｋｇ／ｍ３・日、特に１〜２．５ｋｇ／ｍ３／日、ＢＯＤ負荷０．３〜３ｋｇ／ｍ３・日、特に０．５〜２ｋｇ／ｍ３・日で、ＭＬＳＳ濃度２，０００〜２０，０００ｍｇ／Ｌ、特に４，０００〜１２，０００ｍｇ／Ｌであることが膜濾過性、処理効率の点から好ましい。 Other processing conditions for the aerobic biological treatment tank 2 include a COD Cr load of 0.7 to 5 kg / m 3 · day, particularly 1 to 2.5 kg / m 3 / day, and a BOD load of 0.3 to 3 kg / m 3.・ Day, especially 0.5-2kg / m 3・ day, MLSS concentration is 2,000-20,000mg / L, especially 4,000-12,000mg / L, membrane filtration and treatment efficiency To preferred.
このような本発明の有機物含有排水の処理装置で処理する有機物含有排水としては、通常生物処理される有機物含有排水であれば良く、特に限定されるものではないが、例えば、電子産業排水、化学工場排水、食品工場排水などが挙げられる。例えば、電子部品製造プロセスでは、現像工程、剥離工程、エッチング工程、洗浄工程などから各種の有機性排水が多量に発生し、しかも排水を回収して純水レベルに浄化して再使用することが望まれているので、これらの排水は本発明の処理対象排水として適しており、本発明の有機物含有排水の処理装置の処理水を必要に応じて更に高度処理することにより高純度水を得ることができる。 The organic matter-containing wastewater to be treated by the organic matter-containing wastewater treatment apparatus of the present invention is not particularly limited as long as it is an organic matter-containing wastewater that is usually biologically treated. Examples include factory wastewater and food factory wastewater. For example, in the electronic component manufacturing process, a large amount of various organic wastewater is generated from the development process, peeling process, etching process, cleaning process, etc., and the wastewater can be collected and purified to a pure water level for reuse. These wastewaters are suitable as wastewater to be treated in the present invention, and high-purity water is obtained by further treating the treated water of the organic matter-containing wastewater treatment device of the present invention as necessary. Can do.
このような有機性排水としては例えば、イソプロピルアルコール、エチルアルコールなどを含有する有機性排水、モノエタノールアミン（ＭＥＡ）、テトラメチルアンモニウムハイドロオキサイド（ＴＭＡＨ）などの有機態窒素、アンモニア態窒素を含有する有機性排水、ジメチルスルホキシド（ＤＭＳＯ）などの有機硫黄化合物を含有する有機性排水が挙げられる。 Examples of such organic wastewater include organic wastewater containing isopropyl alcohol, ethyl alcohol, and the like, organic nitrogen such as monoethanolamine (MEA) and tetramethylammonium hydroxide (TMAH), and ammonia nitrogen. Organic waste water and organic waste water containing organic sulfur compounds such as dimethyl sulfoxide (DMSO) can be mentioned.
以下に実施例及び比較例を挙げて本発明をより具体的に説明する。 Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples.
［比較例１、実施例１，２］
下記水質の電子部品製造工場の排水を原水として、図１に示す有機物含有排水の処理装置で処理を行った。
[Comparative Example 1, Examples 1 and 2]
Using the wastewater of the following water quality electronic component manufacturing factory as raw water, treatment was performed with the organic matter-containing wastewater treatment apparatus shown in FIG.
＜原水水質＞
ＣＯＤＣｒ：１,５００〜３，０００ｍｇ／Ｌ（平均２，０００ｍｇ／Ｌ）
Ｔ−Ｎ：３０〜７０ｍｇ／Ｌ（平均５０ｍｇ／Ｌ）
Ｔ−Ｐ：３．０ｍｇ／Ｌ（Ｃａ，Ｍｇ，Ｋ，その他の微量金属とともに栄養剤として添加）
<Raw water quality>
COD Cr : 1,500 to 3,000 mg / L (average 2,000 mg / L)
TN: 30 to 70 mg / L (average 50 mg / L)
TP: 3.0mg / L (added as a nutrient with Ca, Mg, K and other trace metals)
嫌気性生物処理槽１としては、槽容量１０Ｌ（φ１６ｃｍ×Ｈ６０ｃｍの円筒状）のものを用い、水理学的滞留時間：４．８時間、温度：３５℃に加温して処理を行った。
嫌気性生物処理槽１には、ポリプロピレン製円筒状担体（φ３ｍｍ×５ｍｍ）を４Ｌ充填し、ビール工場の排水処理施設のグラニュールを種汚泥として５００ｍＬ投入して２ヶ月馴養の後、処理水を好気性生物処理槽２に導入した。
As the anaerobic biological treatment tank 1, a tank having a tank capacity of 10 L (φ16 cm × H60 cm cylindrical shape) was used, and the treatment was performed by heating to a hydraulic retention time of 4.8 hours and a temperature of 35 ° C.
The anaerobic biological treatment tank 1 is filled with 4 L of a polypropylene cylindrical carrier (φ3 mm × 5 mm), and 500 mL of granule of a wastewater treatment facility in a beer factory is added as seed sludge, and after 2 months acclimatization, treated water is supplied. It introduced into the aerobic biological treatment tank 2.
好気性生物処理槽２としては、槽容量１．５Ｌのものを用い、膜モジュール４としては、中空糸型式のＭＦ膜（旭化成ケミカルズ（株）製「マイクローザＭＦラボモジュール」、ポリフッ化ビニリデン製、孔径０．１０μｍ）を用い、好気性生物処理槽２内の散気管５の上方に浸漬配置した。
As the aerobic biological treatment tank 2, a tank capacity of 1.5 L is used, and as the membrane module 4, a hollow fiber type MF membrane ("Microza MF Lab Module" manufactured by Asahi Kasei Chemicals Co., Ltd.), manufactured by polyvinylidene fluoride , With a pore diameter of 0.10 μm), and was placed so as to be immersed above the
好気性生物処理槽２は、電子部品製造工場排水処理設備の活性汚泥を種汚泥として立ち上げ、膜モジュール４では、６分吸引濾過／２分停止のサイクル、濾過時のフラックス０．４ｍ／日で吸引することにより膜分離処理した。
また、膜間差圧が３０ｋＰａまで上昇したところで、膜モジュール４を引き上げ、薬品洗浄（有効塩素０．３％ＮａＣｌＯ＋ＮａＯＨ（ｐＨ１２に調整）溶液に６時間浸漬）を実施した。
The aerobic biological treatment tank 2 is activated sludge from the wastewater treatment facility of the electronic component manufacturing factory as seed sludge, and the membrane module 4 has a 6-minute suction filtration / 2-minute stop cycle, a filtration flux of 0.4 m / day The membrane was separated by aspiration.
Moreover, when the transmembrane pressure difference increased to 30 kPa, the membrane module 4 was pulled up and chemical cleaning (immersion in an effective chlorine 0.3% NaClO + NaOH (adjusted to pH 12) solution for 6 hours) was performed.
＜比較例１＞
上記条件で処理するに当たり、好気性生物処理槽２から１５０ｍＬ／日で余剰汚泥を引き抜き（汚泥滞留時間＝１０日）、１ヶ月運転した。
<Comparative Example 1>
In the treatment under the above conditions, surplus sludge was extracted from the aerobic biological treatment tank 2 at 150 mL / day (sludge retention time = 10 days) and operated for 1 month.
＜実施例１＞
上記比較例１の運転後、好気性生物処理槽２から７５ｍＬ／日で余剰汚泥を引き抜いたこと（汚泥滞留時間＝２０日）以外は上記比較例１と同様にして、２ヶ月運転した。
<Example 1>
After the operation in Comparative Example 1, the operation was performed for 2 months in the same manner as in Comparative Example 1 except that excess sludge was extracted from the aerobic biological treatment tank 2 at 75 mL / day (sludge retention time = 20 days).
＜実施例２＞
上記実施例１の運転後、好気性生物処理槽２から３０ｍＬ／日で余剰汚泥を引き抜いたこと（汚泥滞留時間＝５０日）以外は上記比較例１と同様にして、３ヶ月運転した。
<Example 2>
After the operation in Example 1, the operation was performed for 3 months in the same manner as in Comparative Example 1 except that excess sludge was extracted from the aerobic biological treatment tank 2 at 30 mL / day (sludge retention time = 50 days).
比較例１及び実施例１，２における膜間差間の経時変化を図２に示す。 FIG. 2 shows the change over time between the differences between the films in Comparative Example 1 and Examples 1 and 2.
比較例１及び実施例１，２共に、嫌気性生物処理槽１では、１０ｋｇ／ｍ３・日のＣＯＤＣｒ負荷に対して、試験期間を通じて９０％前後の除去率が安定して得られ、好気性生物処理槽２の処理水ＣＯＤＣｒは１０ｍｇ／Ｌ以下（平均５．４ｍｇ／Ｌ）で安定して推移した。
比較例１及び実施例１，２において、余剰汚泥引き抜き量の変更後、運転が安定していたと見られる期間の膜間差圧の上昇速度は、比較例１：１．６ｋＰａ／日、実施例１：０．３ｋＰａ／日、実施例２：０．６ｋＰａ／日であり、比較例１ではおよそ１５〜２０日に１回の頻度で薬品洗浄が必要であったのに対し、実施例１，２では薬品洗浄頻度を２ヶ月に１回程度に低減できた。
In both Comparative Example 1 and Examples 1 and 2, the anaerobic biological treatment tank 1 stably obtained a removal rate of around 90% throughout the test period for a COD Cr load of 10 kg / m 3 · day. The treated water COD Cr in the aerobic biological treatment tank 2 was stably changed at 10 mg / L or less (average 5.4 mg / L).
In Comparative Example 1 and Examples 1 and 2, the rate of increase in the transmembrane pressure difference during the period when the operation is considered to be stable after the change of the excess sludge extraction amount is Comparative Example 1: 1.6 kPa / day, Example 1: 0.3 kPa / day, Example 2: 0.6 kPa / day, and Comparative Example 1 required chemical cleaning once every 15 to 20 days, whereas Example 1 In 2, the chemical cleaning frequency could be reduced to about once every two months.
また、嫌気生物処理水のＳＳを分析したところ、嫌気生物処理水には６０〜１００ｍｇ／ＬのＳＳが含まれており、好気性生物処理槽２に常時流入していた。嫌気性物処理水及び好気性生物処理槽汚泥のＳＳ成分の粒径分布を測定したところ、嫌気生物処理水では粒径１０μｍ未満の微細なＳＳ成分が４０％を占めており、比較例１の好気性生物処理槽汚泥でも粒径１０μｍ未満の微細なＳＳ成分が約１０％を占めていた。これに対し、実施例１，２における好気性生物処理槽汚泥では、粒径１０μｍ未満の微細なＳＳ成分がそれぞれ約０．３％、１．２％と著しく少なくなっており、好気性生物処理槽内で微細ＳＳ成分が分解され、膜濾過性の向上につながっていると考えられた。 Moreover, when SS of anaerobic biological treatment water was analyzed, 60-100 mg / L of SS was contained in the anaerobic biological treatment water, and it always flowed into the aerobic biological treatment tank 2. When the particle size distribution of the SS component of the anaerobic material treated water and the aerobic biological treatment tank sludge was measured, the fine SS component having a particle size of less than 10 μm accounted for 40% in the anaerobic biological treated water. Even in the aerobic biological treatment tank sludge, fine SS components having a particle diameter of less than 10 μm accounted for about 10%. On the other hand, in the aerobic biological treatment tank sludge in Examples 1 and 2, the fine SS components having a particle size of less than 10 μm are remarkably reduced to about 0.3% and 1.2%, respectively. It was thought that the fine SS component was decomposed in the tank, leading to an improvement in membrane filterability.
このように、本発明によれば、嫌気性生物処理と膜分離活性汚泥処理を組み合わせた処理において、嫌気性生物処理で生成する微細なＳＳ成分による膜汚染を低減し、膜の洗浄頻度を少なくすると共に膜フラックスを高くして運転することができることが分かる。 As described above, according to the present invention, in the treatment combining the anaerobic biological treatment and the membrane separation activated sludge treatment, the membrane contamination due to the fine SS component generated by the anaerobic biological treatment is reduced, and the membrane washing frequency is reduced. It can be seen that the membrane flux can be increased and the operation can be performed.
１ 嫌気性生物処理槽
２ 好気性生物処理槽
３ 担体
４ 膜モジュール
５ 散気管
1 Anaerobic biological treatment tank 2 Aerobic biological treatment tank 3 Carrier 4
Claims (5)
該嫌気性生物処理工程から流出する嫌気性生物処理水を好気的に生物処理する好気性生物処理工程と、
該好気性生物処理工程の好気性生物処理水を固液分離する膜分離工程とを有する有機物含有排水の処理方法において、
該好気性生物処理工程内における汚泥滞留時間を１５日以上に制御することを特徴とする有機物含有排水の処理方法。 Anaerobic biological treatment process for anaerobically biologically treating organic matter-containing wastewater;
An aerobic biological treatment step for aerobically biologically treating the anaerobic biological treatment water flowing out of the anaerobic biological treatment step;
In the method for treating organic matter-containing wastewater, comprising a membrane separation step for solid-liquid separation of the aerobic biological treatment water of the aerobic biological treatment step,
A method for treating organic matter-containing wastewater, wherein the sludge residence time in the aerobic biological treatment step is controlled to 15 days or more.
該嫌気性生物処理槽から流出する嫌気性生物処理水を好気的に生物処理する好気性生物処理槽と、
該好気性生物処理槽の好気性生物処理水を固液分離する膜分離手段とを有する有機物含有排水の処理装置において、
該好気性生物処理槽内における汚泥滞留時間が１５日以上に制御されることを特徴とする有機物含有排水の処理装置。 An anaerobic biological treatment tank for anaerobically biologically treating organic wastewater,
An aerobic biological treatment tank for aerobically biologically treating anaerobic biological treatment water flowing out of the anaerobic biological treatment tank;
In a treatment apparatus for organic matter-containing wastewater having a membrane separation means for solid-liquid separation of aerobic biological treatment water in the aerobic biological treatment tank,
An apparatus for treating organic matter-containing wastewater, wherein a sludge residence time in the aerobic biological treatment tank is controlled to 15 days or more.
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| JP2007175582A (en) * | 2005-12-27 | 2007-07-12 | Kurita Water Ind Ltd | Apparatus and method for treating wastewater containing organic matter |
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| TWI313187B (en) * | 2003-11-21 | 2009-08-11 | Ind Tech Res Inst | System for the treatment of organic containing waste water |
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| JP2014213320A (en) * | 2013-04-29 | 2014-11-17 | 株式会社明電舎 | Method and device for treating 1,4-dioxane-containing waste water |
| JP2016123920A (en) * | 2014-12-26 | 2016-07-11 | オルガノ株式会社 | Wastewater treatment apparatus and method |
| CN105366806A (en) * | 2015-12-03 | 2016-03-02 | 清华大学 | Anaerobic-micro-aerobic membrane bioreactor and operation method thereof |
| JP2018015689A (en) * | 2016-07-26 | 2018-02-01 | 水ｉｎｇ株式会社 | Organic wastewater treatment facility and operation method thereof |
| JP2019130504A (en) * | 2018-02-01 | 2019-08-08 | オルガノ株式会社 | Water treatment method and water treatment device |
| CN109607766A (en) * | 2018-12-06 | 2019-04-12 | 同济大学 | A kind of start-up method for variable mud age in IFAS process |
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| KR20120112142A (en) | 2012-10-11 |
| TWI596063B (en) | 2017-08-21 |
| TW201300330A (en) | 2013-01-01 |
| CN102730901A (en) | 2012-10-17 |
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