JP5817177B2 - Organic wastewater treatment equipment - Google Patents
Organic wastewater treatment equipment Download PDFInfo
- Publication number
- JP5817177B2 JP5817177B2 JP2011074618A JP2011074618A JP5817177B2 JP 5817177 B2 JP5817177 B2 JP 5817177B2 JP 2011074618 A JP2011074618 A JP 2011074618A JP 2011074618 A JP2011074618 A JP 2011074618A JP 5817177 B2 JP5817177 B2 JP 5817177B2
- Authority
- JP
- Japan
- Prior art keywords
- treatment
- tank
- treatment tank
- organic
- aerobic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
本発明は、有機性排水を嫌気処理し次いで好気処理した処理液を膜により固液分離する生物処理装置に関するものであり、特に有機性排水が、液晶ディスプレイまたは半導体製造工場から排出されるものであって、全有機物のうち炭素数４以下の有機物の割合が７０％以上である場合に好適な有機性排水の処理装置に関する。 The present invention relates to a biological treatment apparatus for subjecting an organic wastewater to an anaerobic treatment and then to a solid-liquid separation of a treatment solution subjected to an aerobic treatment using a membrane. Particularly, the organic wastewater is discharged from a liquid crystal display or a semiconductor manufacturing factory. And it is related with the processing apparatus of the organic wastewater suitable when the ratio of C4 or less organic substances is 70% or more among all the organic substances.
液晶ディスプレイまたは半導体製造工場などの電子産業工場ででは、モノエタノールアミン、テトラメチルアンモニウムヒドロキシド、ジエチレングリコールモノ−Ｎ−ブチルエーテル、イソプロピルアルコールなどプロセス工程で洗浄剤、剥離剤などとして使用される特定の低分子有機物を含む排水が排出される。従来、嫌気処理が適用されている、食品、飲料工場などのデンプン、糖、タンパクなどの高分子有機物を含む排水では、分解の過程で生成する種々の遅分解性成分の一部が処理水に残存することが多いが、電子産業工場排水に含まれる低分子有機物は、遅分解性の中間体を生成することなく、速やかに酢酸、メタンまで分解される。したがって、電子産業工場排水の嫌気処理では、ＢＯＤ３００〜５００ｍｇ／Ｌ程度の排水に対しても９５％以上の高い除去率で処理することができ、処理液は著しく有機物濃度が低くなる(ＢＯＤ２０ｍｇ／Ｌ以下)。 In electronics industry factories such as liquid crystal displays or semiconductor manufacturing factories, certain low concentrations used as cleaning agents, release agents, etc. in process steps such as monoethanolamine, tetramethylammonium hydroxide, diethylene glycol mono-N-butyl ether, isopropyl alcohol Wastewater containing molecular organic matter is discharged. Conventionally, in wastewater containing high-molecular organic substances such as starch, sugar, and protein in food and beverage factories where anaerobic treatment has been applied, some of the various slow-degradable components that are produced during the decomposition process are treated water. Although it often remains, low-molecular-weight organic substances contained in the wastewater from the electronics industry factory are rapidly decomposed into acetic acid and methane without producing a slow-decomposable intermediate. Therefore, in anaerobic treatment of electronic industrial factory wastewater, wastewater having a BOD of about 300 to 500 mg / L can be treated with a high removal rate of 95% or more, and the treatment liquid has a significantly low organic substance concentration (BOD20 mg / L Less than).
このような半導体工場等からの有機性排水を生物処理する装置として、有機性排水を嫌気処理した後、好気処理し、次いで固液分離するものが知られている（特許文献１，２）。特許文献２では、膜を硝化槽内に配置している。
As an apparatus for biologically treating organic wastewater from such semiconductor factories or the like, an apparatus that anaerobically treats organic wastewater, then aerobically treats and then separates into solid and liquid is known (Patent Documents 1 and 2). . In
嫌気処理では、膜汚染の原因となる代謝産物の生成が好気処理よりも少ないので、上記のように嫌気→好気→膜分離のプロセスによると、原水を直接好気処理して膜分離する場合よりも、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。また、嫌気処理を行うため、汚泥発生量の低減、曝気空気量の低減といった効果もある。 Anaerobic treatment produces fewer metabolites that cause membrane contamination than aerobic treatment. As described above, according to the process of anaerobic → aerobic → membrane separation, the raw water is directly aerobically treated for membrane separation. As compared with the case, film contamination is reduced, and the frequency of chemical cleaning of the film can be reduced. In addition, since the anaerobic treatment is performed, there are effects such as reduction of sludge generation amount and reduction of aeration air amount.
生物処理液を膜分離処理する分離膜モジュールには、膜モジュールを曝気槽内に浸漬させて濾過水を吸引する浸漬型と、曝気槽外に設けられた膜モジュールに槽内汚泥を循環し、処理水を吸引する槽外型がある。 In the separation membrane module for membrane separation treatment of the biological treatment liquid, the sludge in the tank is circulated in the immersion module that immerses the membrane module in the aeration tank and sucks the filtered water, and the membrane module provided outside the aeration tank, There is an outside tank type that sucks treated water.
上述の通り、電子産業工場排水の嫌気処理では、ＢＯＤ３００〜５００ｍｇ／Ｌ程度の排水に対しても９５％以上の高い除去率で処理することができ、処理液は著しく有機物濃度が低くなる(ＢＯＤ２０ｍｇ／Ｌ以下)。従って、電子産業排水の嫌気処理の後段の膜分離モジュールとして浸漬型を用いると、膜モジュールを浸漬させるスペースの確保のために曝気槽容量が大きくなり、好気処理槽は極めて低いＢＯＤ負荷及び槽内汚泥濃度で運転されることになる。 As described above, in anaerobic treatment of wastewater from electronic industrial factories, wastewater with a BOD of 300 to 500 mg / L can be treated with a high removal rate of 95% or more, and the treatment liquid has a significantly lower organic matter concentration (BOD20 mg / L or less). Therefore, when the immersion type is used as a membrane separation module subsequent to anaerobic treatment of electronic industrial wastewater, the capacity of the aeration tank increases to secure a space for immersing the membrane module, and the aerobic treatment tank has an extremely low BOD load and tank. It will be operated at the internal sludge concentration.
浸漬型膜モジュールを有した好気処理槽内の汚泥濃度が２，０００ｍｇ／Ｌ以下のように低いと、膜表面に濾過ケーク層が形成されず、逆に目詰まりしやすくなる他、汚泥の引抜き量を少なくして過度にＳＲＴを長くした場合、汚泥が分散化して目詰まりしやすくなる。このように、電子産業排水の嫌気処理の後段に設けた、浸漬型膜モジュールを有する好気処理槽では、膜汚染が激しく、洗浄頻度が増加してしまうという問題があった。 If the sludge concentration in the aerobic treatment tank having a submerged membrane module is as low as 2,000 mg / L or less, a filter cake layer is not formed on the membrane surface, and conversely, clogging tends to occur. When the withdrawal amount is reduced and the SRT is excessively lengthened, sludge is dispersed and clogging is likely to occur. As described above, in the aerobic treatment tank having the immersion type membrane module provided in the subsequent stage of the anaerobic treatment of the electronic industrial wastewater, there is a problem that the membrane contamination is severe and the cleaning frequency increases.
本発明は、有機性排水を嫌気処理する嫌気処理槽と、嫌気処理槽の処理液を好気処理槽で好気処理し、膜分離モジュールで固液分離して処理水を得る排水処理装置において、膜分離モジュールの膜汚染を抑制し、洗浄頻度を少なくすることを目的とする。 The present invention relates to an anaerobic treatment tank for anaerobically treating organic wastewater, and a wastewater treatment apparatus that obtains treated water by aerobic treatment of the treatment liquid in the anaerobic treatment tank and solid-liquid separation with a membrane separation module. The purpose is to suppress membrane contamination of the membrane separation module and reduce the frequency of cleaning.
請求項１の有機性排水の処理装置は、有機性排水を嫌気処理する嫌気処理槽と、嫌気処理槽の処理液を好気処理槽で好気処理し、膜分離モジュールで固液分離して処理水を得る排水処理装置において、該有機性排水の全有機物のうち炭素数４以下の有機物の割合が７０％以上であり、該有機性排水の１〜３０％を、該嫌気処理槽をバイパスさせて該好気処理槽に添加し、該好気処理槽から該嫌気処理槽へ処理液の返送を行わないことを特徴とするものである。
請求項２の有機性排水の処理装置は、有機性排水を嫌気処理する嫌気処理槽と、嫌気処理槽の処理液を好気処理槽で好気処理し、膜分離モジュールで固液分離して処理水を得る排水処理装置において、該有機性排水の全有機物のうち炭素数４以下の有機物の割合が７０％以上であり、該好気処理槽に嫌気処理液以外の有機物を、該好気処理槽のＢＯＤ負荷として０．２〜０．５ｋｇ／ｍ３・ｄ添加し、該好気処理槽から該嫌気処理槽へ処理液の返送を行わないことを特徴とするものである。
The organic waste water treatment apparatus according to claim 1 is an anaerobic treatment tank for anaerobically treating organic waste water, and an aerobic treatment tank for treating liquid of the anaerobic treatment tank, followed by solid-liquid separation with a membrane separation module. In the wastewater treatment apparatus for obtaining treated water, the proportion of organic matter having 4 or less carbon atoms in the total organic matter of the organic wastewater is 70% or more, and 1-30% of the organic wastewater is bypassed the anaerobic treatment tank. Thus, it is added to the aerobic treatment tank, and the treatment liquid is not returned from the aerobic treatment tank to the anaerobic treatment tank .
The organic wastewater treatment apparatus according to
請求項３の有機性排水の処理装置は、請求項１又は２において、前記有機性排水が液晶ディスプレイまたは半導体製造工場から排出されるものであることを特徴とするものである。
Processor of organic waste water according to
本発明は、有機性排水を嫌気処理する嫌気処理槽と、嫌気処理槽の処理液を好気処理槽で好気処理し、膜分離モジュールで固液分離して処理水を得る排水処理装置において、好気処理槽に嫌気性処理液以外の有機物源を添加し、好気汚泥を成長させる。これにより、嫌気処理で生成する微細なＳＳ成分が汚泥フロックに取り込まれ、膜濾過性が改善されるようになり、膜洗浄頻度が少なくなる。 The present invention relates to an anaerobic treatment tank for anaerobically treating organic wastewater, and a wastewater treatment apparatus that obtains treated water by aerobic treatment of the treatment liquid in the anaerobic treatment tank and solid-liquid separation with a membrane separation module. Add organic sources other than anaerobic treatment liquid to the aerobic treatment tank to grow aerobic sludge. Thereby, the fine SS component produced | generated by an anaerobic process is taken in into sludge floc, a membrane filterability comes to improve, and membrane cleaning frequency decreases.
図１は本発明の有機性排水の処理装置のフローを示すものであり、有機性排水は嫌気処理槽１で嫌気処理された後、好気処理槽２に導入され、散気管２ａから散気される空気によって曝気されて好気処理される。好気処理液がポンプ３により槽外の膜モジュール４に供給され、透過水が処理水として取り出される。濃縮水は好気処理槽２に返送される。図１では槽外型膜モジュールとしているが、膜モジュールを好気処理槽２内に浸漬配置してもよい。
FIG. 1 shows the flow of the organic wastewater treatment apparatus of the present invention. The organic wastewater is anaerobically treated in the anaerobic treatment tank 1 and then introduced into the
本発明が処理対象とする有機性排水は、液晶ディスプレイまたは半導体製造工場から排出されるものであって、全有機物のうち炭素数４以下の有機物の割合（重量割合）が７０％以上である排水が好適である。 The organic wastewater to be treated by the present invention is discharged from a liquid crystal display or a semiconductor manufacturing factory, and is a wastewater in which the proportion (weight proportion) of organic substances having 4 or less carbon atoms is 70% or more of all organic substances. Is preferred.
このような炭素数４以下の有機物としては、イソプロピルアルコール（ＩＰＡ）、エチルアルコール、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）、ジメチルスルホキシド（ＤＭＳＯ）などが例示される。 Examples of such organic substances having 4 or less carbon atoms include isopropyl alcohol (IPA), ethyl alcohol, monoethanolamine (MEA), tetramethylammonium hydroxide (TMAH), dimethyl sulfoxide (DMSO) and the like.
嫌気処理槽の処理方式は限定されないが、ＵＡＳＢ、ＥＧＳＢのようなグラニュールを用いたものや、流動床、固定床のような担体を存在させたものが、ＣＯＤｃｒ負荷５ｋｇ／ｍ３・ｄ以上の高負荷処理ができるという点から好ましい。なお、嫌気処理槽の前段に酸生成槽を設けてもよい。 The treatment method of the anaerobic treatment tank is not limited, but those using granules such as UASB and EGSB, and those in which a carrier such as a fluidized bed or a fixed bed is present have a COD cr load of 5 kg / m 3 · d. It is preferable from the point that the above high load processing can be performed. In addition, you may provide an acid production tank in the front | former stage of an anaerobic processing tank.
嫌気性生物処理水を好気的に生物処理するための好気処理槽としては、有機物の分解効率に優れるものであれば良く、既知の好気性生物処理方式の生物反応槽が使用できる。例えば、活性汚泥を槽内に浮遊状態で保持する浮遊方式、活性汚泥を担体に付着させて保持する生物膜方式などを採用することができる。また、生物膜方式では固定床式、流動床式、展開床式など任意の微生物床方式でよく、更に担体として、活性炭、種々のプラスチック担体、スポンジ担体などがいずれも使用できる。 As an aerobic treatment tank for aerobically biologically treating anaerobic biologically treated water, it is sufficient if it is excellent in the decomposition efficiency of organic matter, and a biological reaction tank of a known aerobic biological treatment system can be used. For example, a floating method for holding activated sludge in a suspended state in a tank, a biofilm method for holding activated sludge attached to a carrier, and the like can be employed. The biofilm method may be any microbial bed method such as a fixed bed method, a fluidized bed method, and a developed bed method, and as the carrier, any of activated carbon, various plastic carriers, sponge carriers, and the like can be used.
本発明では、この好気処理槽２に対し、嫌気性処理液以外の有機物源を添加し、好気汚泥を成長させる。これにより、嫌気処理で生成する微細なＳＳ成分が汚泥フロックに取り込まれ、膜濾過性が改善される。
In the present invention, an organic substance source other than the anaerobic treatment liquid is added to the
添加する有機物の例としては、メタノール、酢酸、液糖、魚肉エキスなどが挙げられる。この場合の有機物の添加量は好気処理槽２のＢＯＤ負荷として０．２〜０．５ｋｇ／ｍ３・ｄ程度が好ましい。
Examples of the organic substance to be added include methanol, acetic acid, liquid sugar, fish meat extract and the like. In this case, the addition amount of the organic substance is preferably about 0.2 to 0.5 kg / m 3 · d as the BOD load of the
また、本発明では、この有機物として、有機性排水（原水）の一部を分取し、この分取した原水を、嫌気処理槽１をバイパスさせて好気処理槽２に添加してもよい。この場合、原水流量の１〜３０％特に１〜１０％程度を分取して好気処理槽２に添加することが好ましい。
Moreover, in this invention, as this organic substance, a part of organic waste water (raw water) may be fractionated, and this separated raw water may be added to the
好気処理槽は、ＣＯＤｃｒ負荷０．５〜２ｋｇ／ｍ３・ｄ、特に０．７〜１．５ｋｇ／ｍ３・ｄ（ＢＯＤ負荷０．３〜１．５ｋｇ／ｍ３・ｄ、特に０．５〜１ｋｇ／ｍ３・ｄ）となるようにするのが好ましい。好気処理槽は、ＳＲＴが１０〜２００ｄ、特に１０〜１００ｄとなる範囲で余剰汚泥の引抜きを行い、ＭＬＳＳ濃度2，０００〜１５，０００ｍｇ／Ｌ、特に３，０００〜６，０００ｍｇ／Ｌを維持するようにすることが膜濾過性の点から好ましい。好気処理槽を多段にし、前段を脱窒槽、後段を硝化槽として、硝化槽から脱窒槽に汚泥を循環するようにしてもよい。 The aerobic treatment tank has a COD cr load of 0.5-2 kg / m 3 · d, particularly 0.7-1.5 kg / m 3 · d (BOD load of 0.3-1.5 kg / m 3 · d, especially 0.5 to 1 kg / m 3 · d) is preferable. The aerobic treatment tank extracts excess sludge within a range of SRT of 10 to 200d, particularly 10 to 100d, and has an MLSS concentration of 2,000 to 15,000 mg / L, particularly 3,000 to 6,000 mg / L. It is preferable to maintain it from the viewpoint of membrane filterability. Sludge may be circulated from the nitrification tank to the denitrification tank using aerobic treatment tanks in multiple stages, the first stage being a denitrification tank and the second stage being a nitrification tank.
この実施の形態では、膜モジュール４を槽外型としているので、好気処理槽容積が膜の設置スペースに影響されず、好気処理槽のＢＯＤ負荷、汚泥濃度、ＳＲＴを膜汚染の少ない適切な条件で運転できるようになり、膜洗浄頻度が少なくなる。ただし、前述の通り、膜モジュールは槽内型であってもよい。 In this embodiment, since the membrane module 4 is an outside tank type, the aerobic treatment tank volume is not affected by the installation space of the membrane, and the BOD load, sludge concentration, and SRT of the aerobic treatment tank are appropriately reduced with little membrane contamination. It becomes possible to operate under the necessary conditions, and the frequency of membrane cleaning is reduced. However, as described above, the membrane module may be an in-bath type.
膜分離モジュールの膜はＭＦ、ＵＦが好適であり、平膜、チューブラ膜、中空糸膜などのいずれでもよい。膜面に空気などのガスを散気することで膜表面の掃流速を高め、濾過性を向上することができる。 The membrane of the membrane separation module is preferably MF or UF, and may be any of a flat membrane, a tubular membrane, a hollow fiber membrane, and the like. By sweeping a gas such as air on the membrane surface, the sweep speed of the membrane surface can be increased and the filterability can be improved.
以下、実施例及び比較例について説明する。 Hereinafter, examples and comparative examples will be described.
［実施例１］
図１に示すフローに従って、下記原水を下記条件で処理した。
[Example 1]
According to the flow shown in FIG. 1, the following raw water was treated under the following conditions.
＜原水＞
電子部品製造工場の排水（有機成分ＭＥＡ、ＴＭＡＨ、ＩＰＡ）
水質：ＢＯＤ３５０ｍｇ／Ｌ、Ｔ−Ｎ２０ｍｇ／Ｌ、Ｔ−Ｐ１ｍｇ／Ｌ（その他の無機塩とともに栄養剤として添加）
水量：４．１ｍ３／ｄ
<Raw water>
Wastewater from electronic component manufacturing plants (organic components MEA, TMAH, IPA)
Water quality: BOD 350mg / L, TN 20mg / L, TP 1mg / L (added as a nutrient with other inorganic salts)
Water volume: 4.1 m 3 / d
＜嫌気処理槽＞
槽容量３００Ｌ（φ６００×Ｈ１１００ｍｍの円筒状）
温度２５℃
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６０Ｌ、ポリプロピレン製円筒状担体（φ３ｍｍ×５ｍｍ）を１２０Ｌ投入し、上向流にて通水。２ヶ月馴養の後、処理水を好気槽に導入した。
<Anaerobic treatment tank>
Tank capacity 300L (φ600 × H1100mm cylindrical shape)
Temperature 25 ° C
60L of the granule at the wastewater treatment facility at the beer factory is used as seed sludge, and 120L of polypropylene cylindrical carrier (φ3mm × 5mm) is added, and water is passed in the upward flow. After 2 months of acclimatization, treated water was introduced into the aerobic tank.
＜好気処理槽＞
槽容量１５０Ｌ
温度２５℃
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、ｐＨ６．８になるように２０％ＮａＯＨで調整した。ＳＲＴ５０ｄとなるように汚泥を引抜いた。好気処理槽にメタノールの１０ｗｔ％水溶液を１Ｌ／ｄ添加した。
<Aerobic treatment tank>
Tank capacity 150L
Temperature 25 ° C
The activated sludge of the electronic component manufacturing factory wastewater treatment equipment was started up as seed sludge and adjusted with 20% NaOH so as to have a pH of 6.8. The sludge was pulled out so as to be SRT50d. 1 L / d of a 10 wt% aqueous solution of methanol was added to the aerobic treatment tank.
＜膜モジュール＞
槽外型チューブラＵＦ膜（Ｎｏｒｉｔ製、孔径０．０３μｍ、膜面積５．１ｍ２／本×１本）
好気槽から４．２ｍ３／ｈｒ／本で汚泥（好気処理液）を循環するとともに、モジュール下部より空気を４．２Ｎｍ３／ｈｒ／本導入。
５ｍｉｎ吸引／１０ｓｅｃ逆洗のサイクルで濾過及び逆洗を行った。処理水吸引時流量は０．２３ｍ３／ｈｒ／本、逆洗流量は１．５ｍ３／ｈｒ／本である。吸引終了時の膜間差圧が５０ｋＰａを超えた時点で膜濾過を停止し、薬品洗浄（ＮａＯＣｌ溶液（有効塩素０．３％、ＮａＯＨでｐＨ１２に調整）をモジュールに導入し、２ｈｒ滞留）を行った。
<Membrane module>
Outside-tubular tubular UF membrane (Norit, pore size 0.03 μm, membrane area 5.1 m 2 / piece × 1)
The sludge (aerobic treatment liquid) is circulated from the aerobic tank at 4.2 m 3 / hr / main and air is introduced from the bottom of the module to 4.2 Nm 3 / hr / main.
Filtration and backwashing were performed in a 5 min suction / 10 sec backwashing cycle. When processing water suction flow rate 0.23 m 3 / hr / present backwash flow rate is 1.5 m 3 / hr / present. Membrane filtration is stopped when the transmembrane pressure difference at the end of suction exceeds 50 kPa, and chemical cleaning (NaOCl solution (effective chlorine 0.3%, adjusted to pH 12 with NaOH) is introduced into the module and stays for 2 hr). went.
［実施例２］
メタノールを添加せず、原水の９０％（３．７ｍ３／ｄ）を嫌気処理槽に供給し、残りの１０％（０．４ｍ３／ｄ）と嫌気処理水を好気槽に導入するようにしたこと以外は実施例１と同様にして処理を行った。
[Example 2]
90% (3.7m 3 / d) of raw water is supplied to the anaerobic tank without adding methanol, and the remaining 10% (0.4m 3 / d) and anaerobic water are introduced into the aerobic tank. The treatment was performed in the same manner as in Example 1 except for the above.
［比較例１］
メタノールを添加しなかったこと以外は実施例１と同様にして処理を行った。原水は全量（１００％）嫌気処理槽に供給した。
[Comparative Example 1]
The treatment was performed in the same manner as in Example 1 except that methanol was not added. The whole amount (100%) of raw water was supplied to the anaerobic treatment tank.
［比較例２］
原水の約５０％（２．１ｍ３／ｄ）を嫌気処理槽に供給し、残りの約５０％（２．０ｍ３／ｄ）と嫌気処理水を好気槽に導入するようにしたこと以外は実施例１と同様にして処理を行った。
[Comparative Example 2]
About 50% of the raw water (2.1m 3 / d) is supplied to the anaerobic treatment tank, except that about 50% remaining (2.0m 3 / d) and the anaerobic treatment water was set to be introduced into the aerobic tank Were processed in the same manner as in Example 1.
［結果］
嫌気処理槽では、比較例、実施例のいずれも、試験期間を通じて９５％以上の除去率が安定して得られ、嫌気処理水のＢＯＤは1０ｍｇ／Ｌ前後で、また好気ＭＢＲの処理水ＢＯＤは３ｍｇ／Ｌ以下で安定して推移した。
[result]
In the anaerobic treatment tank, in both the comparative example and the example, a removal rate of 95% or more is stably obtained throughout the test period, the BOD of the anaerobic treated water is around 10 mg / L, and the treated water BOD of the aerobic MBR. Remained stable at 3 mg / L or less.
好気処理槽の運転開始後、膜間差圧の推移を測定し、図２，３に示した。 After the start of the operation of the aerobic treatment tank, the transition of the transmembrane pressure difference was measured and is shown in FIGS.
比較例１ではおよそ１回／３０日の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１回／４０〜５０日程度に低減することができた。嫌気処理水には１５〜４０ｍｇ／ＬのＳＳが含まれており、好気槽に常時流入していた。嫌気処理水および好気槽汚泥のＳＳ成分の粒径分布を測定したところ、嫌気処理水では粒径１０μｍ未満の微細な成分が約４０％を占めており、比較例１では好気槽汚泥でも粒径１０μｍ未満の微細な成分が１０％前後残存していた。これに対し、実施例１、２では粒径１０μｍ未満の成分が１％未満と著しく少なくなっており、好気槽内で微細ＳＳ成分が分解、または汚泥フロックに取り込まれ、膜濾過性の向上につながっていると考えられた。 In Comparative Example 1, chemical cleaning was required about once / 30 days, whereas in Examples 1 and 2, the chemical cleaning frequency could be reduced to about once / 40 to 50 days. The anaerobic treated water contained 15-40 mg / L of SS and was always flowing into the aerobic tank. When the particle size distribution of SS components in anaerobic treated water and aerobic tank sludge was measured, fine components having a particle size of less than 10 μm accounted for about 40% in anaerobic treated water. Fine components having a particle size of less than 10 μm remained around 10%. On the other hand, in Examples 1 and 2, the component having a particle diameter of less than 10 μm is remarkably reduced to less than 1%, and the fine SS component is decomposed in the aerobic tank or taken into the sludge floc, thereby improving the membrane filterability. It was thought that it was connected to.
なお、原水のバイパス量を増やした比較例２では、洗浄頻度は１回／１５日程度と大幅に増加した。槽内の溶解性ＴＯＣ濃度（平均値）が、比較例１の３５ｍｇ／Ｌ、実施例１の５２ｍｇ／Ｌ、実施例２の４５ｍｇ／Ｌに対し、１２０ｍｇ／Ｌと著しく高かったことから、好気槽の有機物負荷が高すぎ、基質摂取時に生成される汚泥代謝産物の分解が不充分で蓄積しているものと考えられる。 In Comparative Example 2 in which the amount of raw water bypass was increased, the cleaning frequency increased significantly to about once / 15 days. The solubility TOC concentration (average value) in the tank was remarkably high at 120 mg / L compared to 35 mg / L in Comparative Example 1, 52 mg / L in Example 1, and 45 mg / L in Example 2. It is considered that the organic matter load in the air tank is too high, and the decomposition of the sludge metabolite produced when the substrate is ingested is insufficiently accumulated.
以上の実施例及び比較例からも明らかな通り、嫌気処理と好気処理及び膜分離を組み合わせた有機性排水処理において、好気処理槽に嫌気処理液以外の有機物を添加することにより、膜モジュールの膜汚染を低減し、膜の洗浄頻度を下げたり、より高いフラックスで運転したりできるようになる。 As is clear from the above examples and comparative examples, in organic wastewater treatment combining anaerobic treatment, aerobic treatment and membrane separation, a membrane module is obtained by adding an organic substance other than the anaerobic treatment liquid to the aerobic treatment tank. The film contamination can be reduced, the frequency of cleaning the film can be reduced, and operation with higher flux can be performed.
１ 嫌気処理槽
２ 好気処理槽
４ 膜分離モジュール
1
Claims (3)
該有機性排水の全有機物のうち炭素数４以下の有機物の割合が７０％以上であり、
該有機性排水の１〜３０％を、該嫌気処理槽をバイパスさせて該好気処理槽に添加し、
該好気処理槽から該嫌気処理槽へ処理液の返送を行わないことを特徴とする有機性排水の処理装置。 In an anaerobic treatment tank that anaerobically treats organic wastewater, and a wastewater treatment apparatus that obtains treated water by aerobic treatment of the treatment liquid in the anaerobic treatment tank and solid-liquid separation with a membrane separation module,
The proportion of the organic matter having 4 or less carbon atoms in the total organic matter of the organic waste water is 70% or more,
1-30% of the organic waste water is added to the aerobic treatment tank by bypassing the anaerobic treatment tank ,
An organic wastewater treatment apparatus , wherein the treatment liquid is not returned from the aerobic treatment tank to the anaerobic treatment tank .
該有機性排水の全有機物のうち炭素数４以下の有機物の割合が７０％以上であり、
該好気処理槽に嫌気処理液以外の有機物を、該好気処理槽のＢＯＤ負荷として０．２〜０．５ｋｇ／ｍ３・ｄ添加し、
該好気処理槽から該嫌気処理槽へ処理液の返送を行わないことを特徴とする有機性排水の処理装置。 In an anaerobic treatment tank that anaerobically treats organic wastewater, and a wastewater treatment apparatus that obtains treated water by aerobic treatment of the treatment liquid in the anaerobic treatment tank and solid-liquid separation with a membrane separation module,
The proportion of the organic matter having 4 or less carbon atoms in the total organic matter of the organic waste water is 70% or more,
Add organic matter other than the anaerobic treatment liquid to the aerobic treatment tank as a BOD load of the aerobic treatment tank of 0.2 to 0.5 kg / m 3 · d ,
An organic wastewater treatment apparatus , wherein the treatment liquid is not returned from the aerobic treatment tank to the anaerobic treatment tank .
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2011074618A JP5817177B2 (en) | 2011-03-30 | 2011-03-30 | Organic wastewater treatment equipment |
| TW101110801A TWI585049B (en) | 2011-03-30 | 2012-03-28 | Organic drainage of the treatment device |
| CN2012100942140A CN102730902A (en) | 2011-03-30 | 2012-03-29 | Processing device for organically dewatering |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2011074618A JP5817177B2 (en) | 2011-03-30 | 2011-03-30 | Organic wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2012206043A JP2012206043A (en) | 2012-10-25 |
| JP5817177B2 true JP5817177B2 (en) | 2015-11-18 |
Family
ID=47186316
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2011074618A Active JP5817177B2 (en) | 2011-03-30 | 2011-03-30 | Organic wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP5817177B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6530188B2 (en) * | 2014-12-26 | 2019-06-12 | オルガノ株式会社 | Waste water treatment apparatus and waste water treatment method |
| JP6612195B2 (en) * | 2016-07-26 | 2019-11-27 | 水ｉｎｇ株式会社 | Organic wastewater treatment facility and operation method thereof |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3203774B2 (en) * | 1992-06-25 | 2001-08-27 | 栗田工業株式会社 | Organic wastewater treatment method and methane fermentation treatment device |
| JP4292610B2 (en) * | 1999-01-22 | 2009-07-08 | 栗田工業株式会社 | Organic wastewater treatment equipment |
| JP5315587B2 (en) * | 2005-12-27 | 2013-10-16 | 栗田工業株式会社 | Apparatus and method for treating wastewater containing organic matter |
| JP4892390B2 (en) * | 2007-04-03 | 2012-03-07 | 株式会社ハウステック | Water treatment apparatus having a solid-liquid separator |
| JP5303862B2 (en) * | 2007-05-11 | 2013-10-02 | 栗田工業株式会社 | Anaerobic treatment method and anaerobic treatment apparatus |
| JP5120106B2 (en) * | 2008-06-27 | 2013-01-16 | 栗田工業株式会社 | Method and apparatus for treating organic alkaline wastewater |
| JP5443057B2 (en) * | 2009-05-29 | 2014-03-19 | オルガノ株式会社 | Anaerobic biological treatment method and anaerobic biological treatment apparatus |
-
2011
- 2011-03-30 JP JP2011074618A patent/JP5817177B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| JP2012206043A (en) | 2012-10-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101274800B (en) | Membrane Separation Activated Sludge Plant | |
| Li et al. | Treatment of synthetic wastewater by a novel MBR with granular sludge developed for controlling membrane fouling | |
| JP5358886B2 (en) | Biological treatment method of water containing organic matter | |
| TWI596063B (en) | Method for treating organic waste water and treating waste containing organic matter | |
| JP2009148714A (en) | Biological treatment method and apparatus for water containing organic matter | |
| KR101956383B1 (en) | Method of treating organic waste water by membrane separator activated sludge device | |
| JP5034778B2 (en) | Membrane separation wastewater treatment method and apparatus | |
| JP2014180629A (en) | Water treatment method and system | |
| JP2012192367A (en) | Treatment device for organic waste water containing nitrogen | |
| Golbabaei Kootenaei et al. | Removal of Nutrients from Hospital Wastewater by Novel Nano-Filtration Membrane Bioreactor (NF-MBR) | |
| JPWO2003043941A1 (en) | Organic wastewater treatment apparatus and method | |
| JP5817177B2 (en) | Organic wastewater treatment equipment | |
| TWI633067B (en) | Method and device for treating organic drainage | |
| TWI585048B (en) | Wastewater containing treatment equipment | |
| JP2012205992A (en) | Treatment apparatus and treatment method of organic matter containing wastewater | |
| JP2012206041A (en) | Treatment method of organic wastewater | |
| Blšt’áková et al. | Domestic wastewater treatment with membrane filtration—two years experience | |
| JP2009189943A (en) | Water treatment method and apparatus | |
| JP2015160202A (en) | Method and apparatus for biological treatment of 1,4-dioxane-containing organic waste water | |
| JP2012206042A (en) | Treatment apparatus of organic wastewater | |
| WO2015002121A1 (en) | Process for purification treatment of wastewater and apparatus for purification treatment of wastewater | |
| TWI585049B (en) | Organic drainage of the treatment device | |
| JP2006055849A (en) | Apparatus and method for treating organic waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20140325 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20150210 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20150403 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20150428 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20150622 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20150901 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20150914 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 5817177 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |