JPH0236000A - Apparatus for treating organic sewage - Google Patents
Apparatus for treating organic sewageInfo
- Publication number
- JPH0236000A JPH0236000A JP63181816A JP18181688A JPH0236000A JP H0236000 A JPH0236000 A JP H0236000A JP 63181816 A JP63181816 A JP 63181816A JP 18181688 A JP18181688 A JP 18181688A JP H0236000 A JPH0236000 A JP H0236000A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- slurry
- nitrification
- denitrification
- activated sludge
- 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.)
- Granted
Links
- 239000010865 sewage Substances 0.000 title claims description 8
- 239000002002 slurry Substances 0.000 claims abstract description 43
- 239000010802 sludge Substances 0.000 claims abstract description 40
- 239000012528 membrane Substances 0.000 claims abstract description 39
- 238000000926 separation method Methods 0.000 claims description 26
- 239000010797 grey water Substances 0.000 claims description 17
- 239000000126 substance Substances 0.000 claims description 3
- 238000000108 ultra-filtration Methods 0.000 abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 24
- 238000000034 method Methods 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000005189 flocculation Methods 0.000 abstract description 5
- 230000016615 flocculation Effects 0.000 abstract description 5
- 230000002378 acidificating effect Effects 0.000 abstract description 4
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- 239000003513 alkali Substances 0.000 abstract 1
- 238000009434 installation Methods 0.000 abstract 1
- 239000010800 human waste Substances 0.000 description 13
- 230000007423 decrease Effects 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 238000005273 aeration Methods 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、し尿、浄化槽汚泥などのし尿汚水を、新規な
概念構成により、合理的に処理し、常に高度に浄化され
た処理水を安定的に得るための装置に関する。[Detailed Description of the Invention] [Field of Industrial Application] The present invention rationally treats human waste water such as human waste and septic tank sludge using a novel conceptual configuration, and provides stable and highly purified treated water at all times. It relates to a device for obtaining the desired results.
〔従来の技術〕゛
し尿系汚水を処理する従来の最も進歩した装置は、し尿
系汚水を雑排水とともに生物学的硝化脱窒素槽へ送り、
そこからの活性汚泥スラリを限外濾過（ＵＦ’）装置へ
送り、そこからの活性汚泥は生物学的硝化脱窒素槽へ返
送し、またそこからの分離水をＦｅ 添加凝集処理を
し、その液をさらに限外濾過装置へ送り、そこからの分
離水を活性炭吸着処理して高度に処理された処理水を得
るという構成をとっており、これはＵＦ膜分離方式と呼
ばれている。[Prior Art] The most advanced conventional equipment for treating human waste water is to send the human waste water together with gray water to a biological nitrification and denitrification tank.
The activated sludge slurry from there is sent to an ultrafiltration (UF') device, the activated sludge from there is returned to the biological nitrification and denitrification tank, and the separated water from there is subjected to Fe addition flocculation treatment and The liquid is further sent to an ultrafiltration device, and the separated water from there is subjected to activated carbon adsorption treatment to obtain highly treated treated water, which is called the UF membrane separation method.
このＵＰ膜分離方式は、活性汚泥及びＦｅ”凝集フロッ
クの固液分離が常に完４−ａあり、ｓｓの沈降性？気に
する必要がないため、維持管理が容易１あるという長所
をもっているため、最近非常に注目されている。This UP membrane separation method has the advantage that solid-liquid separation of activated sludge and Fe" coagulated flocs is always complete 4-a, and maintenance is easy because there is no need to worry about the sedimentation of SS. , has been attracting a lot of attention recently.
しかし、この最新のＵＦ膜分離方式でも、次のような重
大な欠点があり、さらに優れた方式の開発が望まれてい
る。However, even this latest UF membrane separation method has the following serious drawbacks, and the development of an even better method is desired.
（ａ） 活性汚泥のＵＦ膜透過水中に含まれるＣＯＤ
、ＰＯ４３−１色度乞除去するため、Ｆｅ系凝集剤を添
加し、生成フロックを第２のＵＦ膜分離装ｆｇＱ除去し
なければならない。この結果、２段階のＵＦ膜分離装置
が必要となり、設備費、運転費が著しく高くなる。(a) COD contained in activated sludge UF membrane permeated water
In order to remove the chromaticity of PO43-1, an Fe-based flocculant must be added and the generated flocs must be removed using a second UF membrane separator fgQ. As a result, a two-stage UF membrane separation device is required, which significantly increases equipment costs and operating costs.
（ｂ） 汚泥脱水濾液、床洗浄汚水などの雑排水を生
物学的硝化脱窒素僧に流入させて、し尿系汚水と合併処
理するため、生物学的硝化脱窒製槽の活性汚泥が希釈さ
れてＭＬＳＳ濃度が低下し、また液温が低下するのフ硝
化脱窒素反応速度が遅（なる。(b) The activated sludge in the biological nitrification and denitrification tank is diluted because gray water such as sludge dewatering filtrate and floor washing sewage flows into the biological nitrification and denitrification tank and is treated together with human waste water. As the MLSS concentration decreases and the liquid temperature decreases, the nitrification and denitrification reaction rate slows down.
以上のように、従来最新のＵＦ膜分離方式は維持管理性
の向上を確保した反面、運転費、設備費がそれ以前の方
式（例えば低希釈二段活性汚泥法）に比べて著しく高く
なり、しかも生物学的硝化脱窒製槽のＭＬＳＳ低下、水
温低下により硝化脱窒素速度の減少をもたらすという重
大な欠点をもっており、側底理想的処理装置とはいえな
い。As mentioned above, although the latest UF membrane separation method has ensured improved maintenance and management, the operating and equipment costs are significantly higher than previous methods (for example, the low dilution two-stage activated sludge method). Moreover, it has a serious drawback in that the MLSS of the biological nitrification and denitrification tank decreases and the nitrification and denitrification rate decreases due to a decrease in water temperature, so it cannot be said to be an ideal treatment device for the bottom side.
本発明は、このような従来のＵＰ膜分離方式の欠点を完
全に解決するだめの装！？、提供することを目的として
おり、具体的には、
Ｆｌ）ＵＦ膜分離装置の２段階適用を不要にし、１段の
ＵＦ膜分離装＆？し尿の高度処理ケ実現し、設備費、運
転費を大幅に節減する。The present invention is a device that completely solves the drawbacks of the conventional UP membrane separation method! ? , specifically, to eliminate the need for two-stage application of Fl) UF membrane separator and to provide one-stage UF membrane separator &? Achieves advanced treatment of human waste and significantly reduces equipment and operating costs.
（２）雑排水流入による硝化脱窒素反応速度の低下を防
止する。(2) Preventing a decrease in the nitrification and denitrification reaction rate due to the inflow of gray water.
この２点の課題を実現し、従来のＵＦ膜分離方式の欠点
を除去する処理装置を提供することを本発明の課題とし
ている。It is an object of the present invention to provide a processing device that achieves these two problems and eliminates the drawbacks of the conventional UF membrane separation system.
本発明は、有機性汚水を流入させる生物学的硝化脱窒製
槽と、前記生物学的硝化脱窒製槽に後続して前記生物学
的硝化脱窒製槽からの活性汚泥スラリ及び雑排水を流入
させる生物処理槽を設け、さらに前記生物処理槽からの
活有機性汚水を流入させる循環タンクを設け、さらに循
環タンクからの活有機性汚水を流入させるＵＰ又はＭＦ
膜分離装置を設け、生物処理槽とＵＦ又はＭＰ膜分離装
置の中間に活性汚泥スラリに無機凝集剤を注入させる薬
注装置を設け、ＵＦ又はＭＦｉ分離装置で分離された凝
集濃縮スラリの大部分を前記循環タンクへ送る流路と前
記凝集濃縮スラリの残りの一部分を前記生物学的硝化脱
窒製槽へ返送汚泥として返送する流路とを設けたことを
特徴とする有機性汚水の処理装置である。The present invention provides a biological nitrification and denitrification tank into which organic sewage flows, and activated sludge slurry and gray water from the biological nitrification and denitrification tank that follow the biological nitrification and denitrification tank. a biological treatment tank into which the organic wastewater flows, a circulation tank into which the active organic wastewater from the biological treatment tank flows, and an UP or MF into which the active organic wastewater from the circulation tank flows.
A membrane separation device is installed, and a chemical injection device is installed between the biological treatment tank and the UF or MP membrane separation device to inject an inorganic flocculant into the activated sludge slurry, and most of the flocculated concentrated slurry separated by the UF or MFi separation device is An apparatus for treating organic sewage, comprising a flow path for sending the slurry to the circulation tank, and a flow path for returning the remaining part of the flocculated and concentrated slurry to the biological nitrification and denitrification tank as return sludge. It is.
本発明の一実施態様を第１図を参照して説明する。One embodiment of the present invention will be described with reference to FIG.
搬入し尿を除渣したし尿１を無希釈タイプの生物学的硝
化脱窒製槽２に供給し、エアレーションと槽内スラリー
の攪拌機能をもつ循環ポンプ３によって、エジェクター
４から空気５を吸引しつつ硝化脱窒水反応を行わせる。The human waste 1 that has been removed from the carried human waste is supplied to a non-dilution type biological nitrification and denitrification tank 2, and air 5 is sucked from an ejector 4 by a circulation pump 3 that has aeration and stirring functions for the slurry in the tank. Perform nitrification and denitrification water reactions.
この硝化脱窒素槽２が本発明の装置における主たる生物
反応槽である。This nitrification and denitrification tank 2 is the main biological reaction tank in the apparatus of the present invention.
硝化脱窒素槽２内フはし尿中のＢＯＤ、窒素成分の９５
％以上が除去され、硝化脱窒素槽２かも流出する活性汚
泥スラリ６中には微量のＢＯＤ、窒素濃度しか含まれな
い。硝化脱窒素槽としては、生物学的硝化脱窒素処理ｆ
きろものならば何でもよく、回分式、連続式のいずれで
もよく、連続式としては公知のタイプのどれでもかまわ
ない。Nitrification and denitrification tank 2 contains BOD and nitrogen components in human waste of 95%.
% or more is removed, and the activated sludge slurry 6 that also flows out of the nitrification and denitrification tank 2 contains only trace amounts of BOD and nitrogen concentration. As a nitrification and denitrification tank, biological nitrification and denitrification treatment f
Any type of solid material may be used, and either a batch type or a continuous type may be used, and the continuous type may be any known type.
次に、硝化脱窒素槽２の次に設けられた生物処理槽８へ
硝化脱窒素槽２から流出する活性汚泥スラリ６乞送り、
またこの生物処理槽８へ汚泥脱水工程から排出される脱
水濾液、バキュームカー洗車汚水、床洗浄汚水などの雑
排水７を流入させ、前記の活性汚泥スラリ６の活性汚泥
を利用して、雑排水７中の汚濁取分乞生物学的に除去す
る。Next, the activated sludge slurry 6 flowing out from the nitrification and denitrification tank 2 is sent to the biological treatment tank 8 provided next to the nitrification and denitrification tank 2,
In addition, gray water 7 such as dehydrated filtrate discharged from the sludge dewatering process, vacuum car wash sewage, floor washing sewage, etc. is allowed to flow into this biological treatment tank 8, and the activated sludge of the activated sludge slurry 6 is used to generate gray water. 7. Remove the contaminants biologically.
しかして、生物処理槽８から流出ｊる活性汚泥スラリ９
を循環タンク１０に導き、Ｆｅ系又はＡｌ系のような無
機凝集剤１１と、無機凝集剤の添加により活性汚泥スラ
リのｐＨが酸性側に寄り過ぎたときｐＨ’ｆ４〜５，５
に調整するためのアルカリ剤１２を添加し、酸性領域で
凝集処理を行い、凝集スラリ１６をポンプにより限外濾
過（ＵＦ）膜分離装［１４のモジュールに高流速ｆ供給
し、ＳＳ零の完全に清澄なＵＦ膜透過水１５とＵＦ膜に
阻止された凝集濃縮スラリ１６に分離する。無機凝集剤
としてはＦ ｅ ｃ ｌ ｓなどのＦｅ系凝集剤が好ま
しい。凝集濃縮スラリ１６の大部分は循環タンク１０に
循環され、また一部分１７は生物学的硝化脱窒素槽２内
の活性汚泥濃度を所定値（通常１０００（）〜１５００
０１１９／ｌ程度が採用される。）に維持するために返
送されろ。循環タンク１０へ循環される凝集濃縮スラリ
の量は硝化脱窒素槽２へ送られる凝集濃縮スラリ（返送
汚泥）１７の量の２０〜７０倍が効果があり、好ましく
は６０〜４０倍フある。Therefore, the activated sludge slurry 9 flowing out from the biological treatment tank 8
is introduced into the circulation tank 10, and when the pH of the activated sludge slurry becomes too acidic due to the addition of an inorganic flocculant 11 such as Fe-based or Al-based inorganic flocculant, pH'f4~5,5
Add an alkaline agent 12 to adjust the temperature, perform a flocculation treatment in an acidic region, and supply the flocculated slurry 16 at a high flow rate f to an ultrafiltration (UF) membrane separation module [14] using a pump to completely remove SS zero. The water is separated into clear UF membrane permeated water 15 and flocculated concentrated slurry 16 blocked by the UF membrane. As the inorganic flocculant, Fe-based flocculants such as Fecls are preferred. Most of the flocculation and concentration slurry 16 is circulated to the circulation tank 10, and a portion 17 is used to maintain the activated sludge concentration in the biological nitrification and denitrification tank 2 to a predetermined value (usually 1000 () to 1500).
Approximately 0.0119/l is adopted. ) to be returned for maintenance. It is effective that the amount of the flocculated concentrated slurry circulated to the circulation tank 10 is 20 to 70 times the amount of the flocculated concentrated slurry (return sludge) 17 sent to the nitrification and denitrification tank 2, preferably 60 to 40 times the amount.
なお、１８は余剰汚泥ｆあり、脱水機（図示せず）に供
給される。In addition, there is surplus sludge f at 18, which is supplied to a dehydrator (not shown).
また、凝集濃縮スラリ１７のｐＨは４〜５．５と酸性な
ので、し尿の水質特にＭアルカリ度の大小によってはこ
のまま凝集濃縮スラリ１７を硝化脱窒素槽２に返送しつ
づけると、硝化脱窒素槽２内のｐＨが低下し、硝化脱窒
素反応が阻害されることが理論的に起り得るの１、安全
策として流入し尿１、硝化脱窒素槽２内、もしくは凝集
濃縮スラリ（返送汚泥）１７のいずれかにアルカリ剤を
注入する装置を設けておくことが好ましい。図示例は、
アルカリ剤注入装置２０Ｙ返送汚泥流路に設けたもの〒
ある。In addition, since the pH of the flocculated concentrated slurry 17 is acidic at 4 to 5.5, depending on the water quality of the human waste, especially the magnitude of the M alkalinity, if the flocculated concentrated slurry 17 is continued to be returned to the nitrification and denitrification tank 2, the nitrification and denitrification tank It is theoretically possible that the pH in the nitrification and denitrification tank 2 will decrease and the nitrification and denitrification reaction will be inhibited. It is preferable to provide a device for injecting an alkaline agent into either of them. The illustrated example is
Alkaline agent injection device 20Y installed in the return sludge flow path
be.
しかして、ＵＦ膜分離装置から出る完全に清澄なＵＦ膜
透過水、すなわちし尿の高度処理水１５はそのまま〒放
流することが可能フあろが、必要により活性炭吸着塔１
９によりＣＯＤ、色度なさらに除去してもよい。Therefore, the completely clear UF membrane permeated water discharged from the UF membrane separation device, that is, the highly treated human waste water 15, can be discharged as is, but if necessary, the activated carbon adsorption tower 1
9 may further remove COD and chromaticity.
なお、余剰汚泥１７の脱水をフィルタプレス、濾布ヲフ
ィルタエレメントとした濾過機等のケーク濾過機能を有
する脱水機を用いて行うと、余剰汚泥中に無機凝集剤に
入っているためにケーク濾過が行われて脱水分離水は清
澄となり、この分離水は生物処理する必要がな（、この
ため雑排水として生物処理槽８へ送って生物処理する必
要がなく、それに伴いＵＦ膜分離装置へ導び（必要がな
（なり、ＵＦ膜の濾過面積、濾過のための動力を大幅に
節減できる。Note that if the excess sludge 17 is dehydrated using a dehydrator with a cake filtration function, such as a filter press or a filter with a filter cloth as a filter element, cake filtration will occur due to the inorganic flocculant contained in the excess sludge. As a result, the dehydrated and separated water becomes clear, and there is no need to biologically treat this separated water (therefore, there is no need to send it as gray water to the biological treatment tank 8 for biological treatment, and accordingly, it is not necessary to send it to the biological treatment tank 8 as gray water and conduct it to the UF membrane separation device. The filtration area of the UF membrane and the power for filtration can be significantly reduced.
ＵＦ膜分離装置の代りにＭＦ膜を用いたＭＰ膜分離装置
を用いることができる。An MP membrane separation device using an MF membrane can be used instead of the UF membrane separation device.
以上のような本発明の横取におけろ技術的思想の骨子を
要約すると、
（１）硝化脱窒素槽に雑排水？流入させない点、（２）
硝化脱窒素槽に後続して生物処理槽を設け、この生物処
理槽に雑排水を供給して雑排水乞生物処理する点、
（３） 生物処理槽に後続して循環タンクを設け、無
機凝集剤による凝集処理７行う点、
（４）循環タンクに循環される凝集濃縮スラリの一部を
分取して硝化脱窒素槽に供給する点、を有機的に結合し
たことにある。To summarize the gist of the technical ideas regarding the stealing of the present invention as described above, (1) Gray water in the nitrification and denitrification tank? Points to avoid inflow (2)
A biological treatment tank is installed following the nitrification and denitrification tank, and gray water is supplied to this biological treatment tank for biological treatment. (3) A circulation tank is installed following the biological treatment tank to treat inorganic flocculation (4) Part of the flocculated concentrated slurry that is circulated in the circulation tank is separated and supplied to the nitrification and denitrification tank.
本発明では雑排水は硝化脱窒素槽２内に流入させないよ
うにすることにより、硝化脱窒累積２の活性汚泥濃度の
低下及び水温の低下を引き起こさない。In the present invention, gray water is not allowed to flow into the nitrification-denitrification tank 2, so that the activated sludge concentration in the nitrification-denitrification accumulation 2 does not decrease and the water temperature does not decrease.
生物処理槽８は、極めて重要な機能をもっ工おり、これ
に雑排水を受は入れることにより、上記した硝化脱窒素
槽における作用馨生ぜしめ、かっ硝化脱窒素槽２から流
出する活性汚泥スラリ乙に微量残留している窒素成分（
通常４０ｍｙ／ｌ以下）をさらに除去するとともに、雑
排水中の汚濁成分を生物学的に除去する。The biological treatment tank 8 has an extremely important function, and by receiving the gray water, it produces the above-mentioned action in the nitrification and denitrification tank, and the activated sludge slurry flowing out from the nitrification and denitrification tank 2. Nitrogen components remaining in trace amounts in B (
(usually less than 40 my/l) and biologically remove pollutant components in gray water.
また、生物処理槽８かも流出する活性汚泥スラリ９に循
環タンク１０などで無機凝集剤を添加し、またそれに凝
集濃縮スラリを循環添加するから、ＵＦ膜分離装置での
分離が容易になる。In addition, an inorganic flocculant is added to the activated sludge slurry 9 flowing out of the biological treatment tank 8 in a circulation tank 10 or the like, and the flocculated concentrated slurry is added thereto by circulation, so that separation by the UF membrane separator becomes easy.
第１図の処理装置について次のような条件を設定した。 The following conditions were set for the processing apparatus shown in FIG.
（１）硝化脱窒素槽
ＭＬＳＳ＝１２０ｏｏ 〜１３０００１９．／ｌし尿滞
留日数 １０日間
攪拌及び曝気方法
ポンプ循環と空気のエジェクターによる吸引による
（２）生物処理槽
ＭＬＳＳ＝９０００〜９５００１ｇ／Ｖ滞留日数 １
日
雑排水流入量 ０．５Ｑ
（し尿処理量をＱｍ’／日とする）
（３）循環タンク
槽容量 ０．０５Ｑ
ｐＨ自動制御装置設置
Ｆ ｅｃｌ ３ 、 Ｎａ ＯＨ薬注点配備凝集ｐＨ４
〜５に制御
凝集濃縮スラリの循環量 ２０Ｑ
（４）ＵＦ膜分離装置
型式 チューブラ−型、クロスフローフィルトレージ
ョン方式
ＵＦ材質 ポリアクリロニトリル
分画分子量 ５００００’ （公称値）モジュール内液
流速 ２．５ ｍ ／ ｓｅｃ透過流速 １．２ｍ
’／ｆｒｌ・膜・日ＵＦ膜分離スラリ
固形物濃度 ２０ＫＰ ／ｒｒｌ
ＵＰ膜分離スラリの硝化脱窒素槽への
返送流量 ０．６〜０．７ Ｑｍ’／日以上の設計条
件及び運転条件で下表の水質の除渣し尿を処理した。(1) Nitrification and denitrification tank MLSS = 120oo ~ 1300019. /l Night soil retention days 10 days Stirring and aeration method By pump circulation and suction with air ejector (2) Biological treatment tank MLSS = 9000-95001 g/V retention days 1
Daily wastewater inflow 0.5Q (The amount of human waste treated is Qm'/day) (3) Circulation tank capacity 0.05Q Automatic pH control device installed Fecl 3, NaOH chemical injection point installed Coagulation pH 4
~5 Controlled coagulation concentration slurry circulation rate 20Q (4) UF membrane separator type Tubular type, cross-flow filtration method UF material Polyacrylonitrile molecular weight cut off 50000' (nominal value) Liquid flow rate in module 2.5 m /sec permeation flow rate 1.2m
'/frl/membrane/day UF membrane separation slurry solids concentration 20KP/rrl Return flow rate of UP membrane separation slurry to nitrification and denitrification tank 0.6 to 0.7 Qm'/day or more under design and operating conditions Surface water quality was removed and human urine was treated.
硝化脱窒素槽から流出する活性汚泥スラリと水量［］、
５Ｑ（ＢＯＤ４００〜５００肩Ｖ／ｌ、Ｔ−Ｎ５０〜１
００ｍｙ／ｌ ）の雑排水（各種洗浄汚水と汚泥脱水法
ｇ、）とを、生物処理槽に流入させて、嫌気、好気を反
復させて生物処理したのち、この槽から流出するＭＬＳ
３９０００〜９５００叩／ｌの活性汚泥スラリに対し、
ＦｅＣｌ３を２０００〜２５００８９／１とＮａＯＨを
５００〜６００１９／７添加し、ｐ Ｈ４〜５の条件′
ｔ％凝集処理した後、ＵＦ膜分離装置に供給した。この
結果、ＵＦ膜透過水の水質は次のように極めて高度に浄
化されていた。Activated sludge slurry and water volume flowing out from the nitrification and denitrification tank [],
5Q (BOD400-500 shoulder V/l, T-N50-1
00 my/l) of gray water (various washing sewage and sludge dewatering method g) is flowed into a biological treatment tank, subjected to biological treatment by repeating anaerobic and aerobic processes, and then MLS flowing out from this tank.
For activated sludge slurry of 39,000 to 9,500 per liter,
Add FeCl3 from 2000 to 250,089/1 and NaOH from 500 to 60,019/7 and set pH to 4 to 5.
After t% aggregation treatment, it was supplied to a UF membrane separation device. As a result, the quality of the water permeated through the UF membrane was extremely purified as shown below.
〔発明の効果〕− 本発明は、次のような効果を有する。[Effects of the invention] - The present invention has the following effects.
（１） １段のＵＦｌ［［Ｉ装ｆｌＫＪｌ、ＳＳ、Ｂ
ＯＤ、ＣＯＤ、窒素、色度、ＰＯ４５−がよく除去され
て、極めて清澄な高度処理水が得られる。(1) 1 stage UFl [[I unit flKJl, SS, B
OD, COD, nitrogen, chromaticity, and PO45- are well removed, resulting in extremely clear highly treated water.
このため、ＵＦ膜分離装置を２段用いる必要はなく、１
段ですむ。Therefore, there is no need to use two stages of UF membrane separation equipment;
It only takes steps.
（２）雑排水を生物学的硝化脱窒素槽に流入させないた
め、核種において活性汚泥ＭＬＳＳ濃度の希訳がなく、
また水温の低下がないため、硝化脱窒製反応が低下せず
、生物処理が順調に行われる。(2) Since gray water is not allowed to flow into the biological nitrification and denitrification tank, there is no reduction in activated sludge MLSS concentration in terms of nuclides.
Furthermore, since there is no drop in water temperature, nitrification and denitrification reactions do not drop, and biological treatment is carried out smoothly.
（３）従来のようにＵＦ膜分離スラリの大部分を硝化脱
窒素槽に循環させることはなく、ＵＦ膜分離装置で分離
された凝集濃縮スラリの大部分を、生物処理槽に後続し
て設ゆられた循環タンクに循環させ、一部のみを硝化脱
窒素槽に循環させるようにしたので、ｐＨが低い凝集濃
縮スラリの流入に起因する硝化脱窒素槽内液のｐＨ低下
を引き起すことがない。したがって、硝化脱窒製反応の
低下を招かない。(3) Instead of circulating most of the UF membrane separated slurry to the nitrification and denitrification tank as in the past, most of the flocculated and concentrated slurry separated by the UF membrane separation device is subsequently placed in the biological treatment tank. Since the slurry is circulated through the shaken circulation tank and only a portion is circulated to the nitrification and denitrification tank, the pH of the solution in the nitrification and denitrification tank will not decrease due to the inflow of the coagulated and concentrated slurry, which has a low pH. do not have. Therefore, the nitrification and denitrification reaction does not deteriorate.
第１図は、本発明の処理装置の概要図である。
１・・・し尿 ２・・・生物学的硝化脱窒素槽
７・・・雑排水 ８・・・生物処理槽１０・・・
循環タンク １１・・・無機凝集剤１４・・・ＵＦ膜
分離装置FIG. 1 is a schematic diagram of a processing apparatus of the present invention. 1... Human waste 2... Biological nitrification and denitrification tank 7... Gray water 8... Biological treatment tank 10...
Circulation tank 11... Inorganic flocculant 14... UF membrane separation device
Claims (1)
生物学的硝化脱窒素槽に後続して前記生物学的硝化脱窒
素槽からの活性汚泥スラリ及び雑排水を流入させる生物
処理槽を設け、さらに前記生物処理槽からの活性汚泥ス
ラリを流入させる循環タンクを設け、さらに循環タンク
からの活性汚泥スラリを流入させるＵＦ又はＭＦ膜分離
装置を設け、生物処理槽とＵＦ又はＭＦ膜分離装置の中
間に活性汚泥スラリに無機凝集剤を注入させる薬注装置
を設け、ＵＦ又はＭＦ膜分離装置で分離された凝集濃縮
スラリの大部分を前記循環タンクへ送る流路と前記凝集
濃縮スラリの残りの一部分を前記生物学的硝化脱窒素槽
へ返送汚泥として返送する流路とを設けたことを特徴と
する有機性汚水の処理装置。a biological nitrification-denitrification tank into which organic sewage flows; and a biological treatment tank into which activated sludge slurry and gray water from the biological nitrification-denitrification tank follow the biological nitrification-denitrification tank. A circulation tank into which the activated sludge slurry from the biological treatment tank flows is provided, and a UF or MF membrane separation device into which the activated sludge slurry from the circulation tank flows into the biological treatment tank and the UF or MF membrane separation device. A chemical dosing device for injecting an inorganic flocculant into the activated sludge slurry is provided between the two, and a flow path for sending most of the flocculated concentrated slurry separated by the UF or MF membrane separation device to the circulation tank, and the remainder of the flocculated concentrated slurry. A flow path for returning a portion of the sludge to the biological nitrification and denitrification tank as return sludge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63181816A JPH0236000A (en) | 1988-07-22 | 1988-07-22 | Apparatus for treating organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63181816A JPH0236000A (en) | 1988-07-22 | 1988-07-22 | Apparatus for treating organic sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0236000A true JPH0236000A (en) | 1990-02-06 |
| JPH0433519B2 JPH0433519B2 (en) | 1992-06-03 |
Family
ID=16107332
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63181816A Granted JPH0236000A (en) | 1988-07-22 | 1988-07-22 | Apparatus for treating organic sewage |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0236000A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05185093A (en) * | 1992-01-10 | 1993-07-27 | Ngk Insulators Ltd | Method for purifying water by using membrane |
| JPH0824594A (en) * | 1994-07-22 | 1996-01-30 | Toto Ltd | Operation of filter |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56129084A (en) * | 1980-03-13 | 1981-10-08 | Ebara Infilco Co Ltd | Disposal of organic waste water containing phosphoric acid |
| JPS60153999A (en) * | 1984-01-24 | 1985-08-13 | Ebara Infilco Co Ltd | Treatment of waste water |
-
1988
- 1988-07-22 JP JP63181816A patent/JPH0236000A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56129084A (en) * | 1980-03-13 | 1981-10-08 | Ebara Infilco Co Ltd | Disposal of organic waste water containing phosphoric acid |
| JPS60153999A (en) * | 1984-01-24 | 1985-08-13 | Ebara Infilco Co Ltd | Treatment of waste water |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05185093A (en) * | 1992-01-10 | 1993-07-27 | Ngk Insulators Ltd | Method for purifying water by using membrane |
| JPH0824594A (en) * | 1994-07-22 | 1996-01-30 | Toto Ltd | Operation of filter |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0433519B2 (en) | 1992-06-03 |
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