JPH029497A - Treating equipment for excretion-series sewage - Google Patents
Treating equipment for excretion-series sewageInfo
- Publication number
- JPH029497A JPH029497A JP63159417A JP15941788A JPH029497A JP H029497 A JPH029497 A JP H029497A JP 63159417 A JP63159417 A JP 63159417A JP 15941788 A JP15941788 A JP 15941788A JP H029497 A JPH029497 A JP H029497A
- Authority
- JP
- Japan
- Prior art keywords
- biological treatment
- treatment tank
- tank
- activated sludge
- separation
- 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 abstract description 6
- 238000011282 treatment Methods 0.000 claims abstract description 73
- 239000010802 sludge Substances 0.000 claims abstract description 47
- 239000002002 slurry Substances 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 239000002351 wastewater Substances 0.000 claims abstract description 4
- 238000000926 separation method Methods 0.000 claims description 46
- 239000010800 human waste Substances 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 229920000642 polymer Polymers 0.000 claims description 6
- 238000005189 flocculation Methods 0.000 claims description 3
- 230000016615 flocculation Effects 0.000 claims description 3
- 230000001546 nitrifying effect Effects 0.000 claims description 2
- 239000002689 soil Substances 0.000 claims description 2
- 239000012528 membrane Substances 0.000 abstract description 31
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 3
- 239000008394 flocculating agent Substances 0.000 abstract 2
- 230000000802 nitrating effect Effects 0.000 abstract 2
- 238000013019 agitation Methods 0.000 abstract 1
- 230000029142 excretion Effects 0.000 abstract 1
- 239000010797 grey water Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005273 aeration Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000010130 dispersion processing Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 235000012254 magnesium hydroxide Nutrition 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
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、し尿と浄化槽汚泥との混
合液などのいわゆるし尿系汚水の処理装置に関するもの
であり、特にし尿系汚水を生物処理し、高度に浄化する
ことができる処理装置に関するもの〒ある。[Detailed Description of the Invention] [Field of Industrial Application] The present invention relates to a treatment device for so-called human waste sewage such as human waste, septic tank sludge, and a mixture of human waste and septic tank sludge. There are some related to processing equipment capable of biological treatment and high purification.
し尿系汚水は従来生物処理やその他の処理により浄化さ
れている。その処理の中、現在最も進歩しているし尿処
理装置を第２図に示す。Human waste water is conventionally purified by biological treatment or other treatments. Among these treatments, the most advanced human waste treatment equipment at present is shown in Figure 2.
第２図の処理装置は、し尿のＵＦ膜分離装置と呼ばれて
おり、ＳＳの分離が常に完譬フあるから、現在大きな注
目を浴びている最も新しいし尿処理装置である。The processing device shown in FIG. 2 is called a UF membrane separation device for human waste, and is the newest human waste processing device that is currently attracting a lot of attention because the separation of SS is always perfect.
第２図の処理装置では、し尿系汚水１と雑排水８をまず
生物処理槽２〒生物学的硝化脱窒素処理した後、この生
物処理槽から流出する活性汚泥スラリー６の全量を限外
濾過（ＵＦ）膜分離装置Ｒ２５により固液分離し、分離
した活性汚泥２６を前記の生物処理槽へ返送する構成を
根幹とするものである。そして、ＳＳ零のＵＦ膜透過液
はＦｅ 系凝集剤が添加され、ＣＯＤ、色度、ＰＯ４
δ−が凝集された後、第２のＵＦ膜分離装置１５により
＃集フロック１７が完全に分離され、清澄な透過水１６
となる。In the treatment equipment shown in Fig. 2, human waste sewage 1 and miscellaneous wastewater 8 are first subjected to biological nitrification and denitrification treatment in a biological treatment tank 2, and then the entire amount of activated sludge slurry 6 flowing out from this biological treatment tank is ultrafiltered. (UF) The basic structure is that solid-liquid separation is performed by a membrane separator R25 and the separated activated sludge 26 is returned to the biological treatment tank. Then, an Fe-based flocculant is added to the SS zero UF membrane permeate, and COD, chromaticity, PO4
After the δ- is aggregated, the #collected flocs 17 are completely separated by the second UF membrane separator 15, and clear permeated water 16 is obtained.
becomes.
すなわち、第２図の処理装置は、活性汚泥分離用と凝集
７０ツク分離用の２つの工程ＫＵＦ膜を適用することを
最大の特徴とするものである。That is, the main feature of the treatment apparatus shown in FIG. 2 is that it uses two-step KUF membranes, one for activated sludge separation and one for flocculation separation.
しかしながら、このＵＦ［分離装置を用いた処理袋［−
？も、次のような問題点が未解決であり、需用者側から
さらに優れた開発が切望されている。However, this UF [processing bag using a separation device]
? However, the following problems remain unresolved, and users are eagerly awaiting even better development.
■ ＵＦ膜分離装置において粘性の高い汚泥を固液分離
するＫは装置費の高額なＵＦ膜モ、ジュール内を２〜３
ｍ／ｓｅｃという高流速）分離すべき液を通過させなけ
れば、実用可能な透過流束（Ｆｌｕｘ）を得ることが１
きない。この結果、ＵＦ膜モジュール内での損失水頭が
高いことと重なって、ポンプの所要規模、動力が非常に
大きいという重大な欠点がある。■K for solid-liquid separation of highly viscous sludge in UF membrane separation equipment is the UF membrane module, which has high equipment costs, and requires 2 to 3 joules.
If the liquid to be separated is not passed through (high flow rate of m/sec), it is difficult to obtain a practical permeation flux (Flux).
I can't. As a result, in addition to the high head loss within the UF membrane module, there is a serious drawback that the required size and power of the pump are very large.
■ ＵＦ模分離装置を活性汚泥分離用と凝集分離用の両
方の工程忙適用しているために、さらに消費エネルイー
と設備費力１倍増してしまう。■ Since the UF simulated separation equipment is used in both processes for activated sludge separation and coagulation separation, the energy consumption and equipment cost increase by a factor of 1.
■ 生物学的硝化脱窒素をする生物処理槽から流出する
活性汚泥スラリーの全景をＵＦ膜に供給して活性汚泥を
固液分離しているため、ＵＦ膜の所要面積が多（、設備
費がかさむほか、必然的にＵＦ膜に活性汚泥スラリーを
供給するポンプの動力費と設備費が大きいという欠点を
もっている。■ The entire activated sludge slurry flowing out from the biological treatment tank for biological nitrification and denitrification is supplied to the UF membrane to separate the activated sludge into solid and liquid, which requires a large area (and equipment costs). In addition to being bulky, it also has the disadvantage of requiring large power and equipment costs for the pump that supplies the activated sludge slurry to the UF membrane.
■ ＵＦ膜による分離工程力１複数あるため、膜汚染防
止用のＮａ０（ＪなどＫよる薬品洗浄操作が煩雑になる
。■ Since there are multiple separation processes using UF membranes, cleaning operations using chemicals such as Na0 (K) to prevent membrane contamination become complicated.
■ ２つのＵＰ膜分離装置から排出される余剰活性汚泥
と凝集汚泥の両者を脱水するため、脱水助剤（カーゼン
ｌリマーなど）を多量に必要とし、運転経費がさらに増
加する。■ In order to dewater both the surplus activated sludge and flocculated sludge discharged from the two UP membrane separation devices, a large amount of dewatering aid (such as Kazenl remer) is required, further increasing operating costs.
■ ＵＦ膜の耐用年数は２〜３年しがないため、膜の交
換コストが高い。ＵＦ膜分離工程を２段設けている従来
装置では膜面積が大きくなるため、膜交換コストはかな
つの＠になる。■ The service life of a UF membrane is only two to three years, so the cost of replacing the membrane is high. In conventional equipment that has two stages of UF membrane separation processes, the membrane area becomes large, so the cost of replacing the membrane becomes significant.
以上のよ５な０〜０項の要因が重なってくるため、上記
のＵＦ膜分離装置を用いるし尿系汚水処理装置は、設備
費、維持管理費がＵＦ膜処理方式が９．場する以前の処
理装置（例えば低希釈散化処理装置）よりもむしろ増加
し、需用者忙とって経費負担が上昇するという問題点を
生じている。Because the factors listed in the above five items 0 to 0 overlap, the equipment cost and maintenance cost of the human waste wastewater treatment equipment using the above-mentioned UF membrane separation equipment is 9. This has resulted in an increase in the number of processing equipment compared to the previous processing equipment (for example, low dilution dispersion processing equipment), which has created a problem in that users are busy and the cost burden has increased.
すなわち、従来のＵＦ膜分離方式は、し尿処理に限外濾
過という先端技術を導入し、ＳＳの分離効率の安定性を
高めたというプラスの効果をもたらしたが、その反面し
尿処理装置全体の設備費の増加を引きおこすという重大
なマイナス効果を引き起した。In other words, the conventional UF membrane separation method introduced cutting-edge technology called ultrafiltration for human waste treatment, which had the positive effect of increasing the stability of SS separation efficiency, but on the other hand, the overall human waste treatment equipment equipment This had the significant negative effect of causing an increase in costs.
本発明は、上述したＵＦ膜分離方式の欠点を太・福て改
善し、し尿処理装置の設備費と運転経費を著しく低下さ
せるとともに、従来のＵＦ膜分離方式と同様に高い処理
効率を確保し、常圧安定して良好な処理水質を得る処理
装置の開発を課題としている。The present invention improves the above-mentioned shortcomings of the UF membrane separation system, significantly reduces equipment costs and operating costs of human waste treatment equipment, and ensures high treatment efficiency similar to the conventional UF membrane separation system. , our goal is to develop a treatment device that can stably maintain normal pressure and produce good quality treated water.
すなわち、本発明はなるぺ＜ＵＦ膜分離装置を用いない
で高い処理効率と良好な水質を得ようとすることを課題
としている。That is, an object of the present invention is to obtain high treatment efficiency and good water quality without using a UF membrane separation device.
本発明は、し尿系汚水を生物学的に硝化脱窒素処理する
第１の生物処理槽を設け、また前記生物処理槽から流出
する活性汚泥スラリーを生物処理する第２の生物処理槽
を設けると共に、第１の生物処理槽内にある、もしくは
同槽から流出する活性汚泥スラリーの一部に高分子凝集
剤を添加し、主属フロックをスクリーン分離する分離装
置を設け、前記分離装置からの分離汚泥を第１の生物処
理槽へ返送する系路と前記分離装置からの分離液を第２
の生物処理槽に供給する系路な設け、第２の生物処理槽
からの流出液に無機系凝集剤を添加して凝集分離する固
液分離装置を設けたことを特徴とするし尿系汚水の処理
装置である。The present invention provides a first biological treatment tank for biologically nitrifying and denitrifying human waste water, and a second biological treatment tank for biologically treating activated sludge slurry flowing out from the biological treatment tank. , a polymer flocculant is added to a part of the activated sludge slurry in or flowing out from the first biological treatment tank, and a separation device is provided to screen and separate the main flocs, and separation from the separation device is provided. A system for returning sludge to the first biological treatment tank and a system for returning the separated liquid from the separation device to the second biological treatment tank.
A system for supplying night soil wastewater to a second biological treatment tank, and a solid-liquid separator for adding an inorganic coagulant to the effluent from the second biological treatment tank for flocculation separation. It is a processing device.
この処理装置においては、第２の生物処理槽へし尿処理
施設の運転に伴って発生する各種雑排水（バキュームカ
ー洗浄汚水、未洗浄汚水、汚泥脱水分離水など）を供給
するよう圧してもよい。従平技術においてはこの雑排水
は第１の生物処理槽に供給せざるを得ない。In this treatment device, pressure may be applied to supply various types of gray water (vacuum car wash sewage, unwashed sewage, sludge dewatered water, etc.) generated in conjunction with the operation of the human waste treatment facility to the second biological treatment tank. . In the Shuhei technology, this gray water has no choice but to be supplied to the first biological treatment tank.
また、第２の生物処理槽から流出する流出液に無機凝集
剤を添加して凝集したものを分離する固液分離装置とし
ては、ＵＦ膜分離装置又はＭＰＦｘ分離装置、あるいは
沈降分離装置を用いることがｒ！きる。In addition, as a solid-liquid separation device that adds an inorganic flocculant to the effluent flowing out from the second biological treatment tank and separates the flocculated product, a UF membrane separation device, an MPFx separation device, or a sedimentation separation device may be used. Ga r! Wear.
以下実施例により本発明を具体的に説明する。 The present invention will be specifically explained below using Examples.
ただし、本発明は実施例のみに限定されるものではない
。However, the present invention is not limited only to the examples.
実施例１ 第１図にこの実施例の態様を示す。Example 1 FIG. 1 shows an aspect of this embodiment.
除潰し尿１を生物学的硝化脱窒素処理をする第１の生物
処理槽２に供給する。処理槽２の型式としては、公知の
硝化液循環型、ステップ屋、−槽式などの任意のタイプ
を採用してもよい。図示例は一槽式の例ｆある。６はエ
アレーションと槽内攪拌用の循環ポンプ！あり、４はエ
ジェクター５は吸引される空気ｆある。The crushed urine 1 is supplied to a first biological treatment tank 2 that performs biological nitrification and denitrification treatment. As the type of the treatment tank 2, any type such as the known nitrification liquid circulation type, step shop, or tank type may be adopted. The illustrated example is a one-tank type example f. 6 is a circulation pump for aeration and stirring inside the tank! 4, the ejector 5 sucks air f.
し尿１は生物処理槽２−１’無希釈で硝化脱窒素処理さ
れた後、同槽２から流出する大部分の活性汚泥スラリー
６ （ＭＬＳＳ ８０００〜１ｓｏｃ＋ｏ■／！程度）
を流路から後続する第２の生物処理槽７に流入させる。The human waste 1 is subjected to nitrification and denitrification treatment without dilution in the biological treatment tank 2-1', and then most of the activated sludge slurry 6 flowing out from the biological treatment tank 2-1' is activated sludge slurry 6 (MLSS 8000~1soc+o/!)
is caused to flow into the subsequent second biological treatment tank 7 from the flow path.
一方、生物処理槽２から活性汚泥の一部１８を抜き出し
、この活性汚泥に薬注装［１９かも高分子凝集剤を注入
する。高分子凝集剤としてはカチオン系あるいはカチオ
ン系とアニオン系を併用し、あるいはこれらとＦｅ、Ａ
Ｉ系凝集剤と併用してもよい。活性汚泥スラリーは高分
子凝集剤の添加により攪拌槽２０でフロックを形放し、
これはスクリーン分離装［２１でフロックを分離する。On the other hand, a portion 18 of the activated sludge is extracted from the biological treatment tank 2, and a polymer flocculant is injected into the activated sludge. As a polymer flocculant, a cation type, a combination of a cation type and an anion type, or a combination of these and Fe, A
It may be used in combination with an I-type flocculant. The activated sludge slurry is treated with a polymer flocculant to form flocs in the stirring tank 20.
This separates the flocs in a screen separator [21].
スクリーン分離装置２１は、目開きα５〜１．０ｍｍ程
度のウェッジワイヤタイプの傾斜型又は回転ドラム型が
よい。この実施例ｆは傾斜型ウェッジワイヤスクリーン
を用いた。分離フロック２２は第１の生物処理槽２内の
活性汚泥濃度を所定値に維持するためにリサイクルされ
る。スクリーン分離装置２１において分離された、ＳＳ
をはとんど含まない液２３は生物処理槽２から流出する
活性汚泥スラリー６と混合し、第２の生物処理槽７に送
られる。The screen separation device 21 is preferably a wedge wire type inclined type or a rotating drum type with an opening of about 5 to 1.0 mm. This Example f used an inclined wedge wire screen. The separated flocs 22 are recycled to maintain the activated sludge concentration in the first biological treatment tank 2 at a predetermined value. SS separated in the screen separation device 21
The liquid 23 containing almost no .
第２の生物処理槽７には場内から発生する雑排水８を流
入させるようにしである。この生物処理槽７は、活性汚
泥スラリー６とスクリーン分離液２３との混合液中に少
量残留する窒素分及び雑排水８中のＢＯＤ、窒素成分を
生物学的に除去する機能をもっている。生物処理槽７の
型式は硝化、脱窒素を行うことが可能な任意のタイプを
採用できるが、この実施例では空気９をＯＮ、ＯＦＦさ
せ、槽内に嫌気、好気条件を交互に設定する一槽式な用
いた。Gray water 8 generated from within the plant is allowed to flow into the second biological treatment tank 7. This biological treatment tank 7 has a function of biologically removing a small amount of nitrogen remaining in the mixed liquid of the activated sludge slurry 6 and the screen separation liquid 23, as well as BOD and nitrogen components in the gray water 8. The biological treatment tank 7 can be of any type that can perform nitrification and denitrification, but in this embodiment, the air 9 is turned on and off to alternately set anaerobic and aerobic conditions in the tank. A one-tank type was used.
しかして、生物処理槽７から流出する活性汚泥スラリー
１０を貯槽１１に導びき、無機凝集剤１２と凝集ｐＨｉ
！１４整用のアルカリ剤１３を添加して凝集させろ。無
機凝集剤としては、ＸＰｅＣ１６１，ｙＢ７硫酸！ｊＩ
ｃ２鉄、ＰＡＣ，Ａｌｕｍなどを用いることが１き、ア
ルカリ剤としては、ＮａＯＨ，Ｃａ０Ｈ。The activated sludge slurry 10 flowing out from the biological treatment tank 7 is guided to the storage tank 11, and the inorganic flocculant 12 and the flocculated pH
! 14 Add alkali agent 13 for cleaning and coagulate. As an inorganic flocculant, XPeC161, yB7 sulfuric acid! jI
C2 iron, PAC, Alum, etc. can be used, and the alkaline agent is NaOH, Ca0H.
Ｍｇ（ＯＨ）２などを用いることができる。凝集スラリ
ーをポンプ１４によってＵＦ膜分離装置１５内に供給し
、凝集フロックを完全に濾過分離し、分離水１６と分離
汚泥１７に分離する。この固液分離はＵＦａ分離装［Ｖ
ｃよらず、ＭＦ膜分離装置、沈降分離、浮上分離、遠心
分離によって行うこともできる。分離水１６はし尿の高
度処理水としてそのまま放流することも〒きるが、さら
に高度に処理する場合には活性炭吸着器２４に通して放
流する。Mg(OH)2 or the like can be used. The flocculated slurry is supplied into the UF membrane separator 15 by the pump 14, and the flocs are completely filtered and separated into separated water 16 and separated sludge 17. This solid-liquid separation is performed using the UFa separator [V
It can also be carried out by using a MF membrane separator, sedimentation separation, flotation separation, or centrifugation. The separated water 16 can be discharged as is as highly treated human waste water, but if it is to be further treated, it is passed through an activated carbon adsorber 24 and discharged.
一方、ＵＦ膜分輪装［１５で分離した汚泥の大部分は循
環汚泥１７′として貯槽１１に循環され、他の残りは余
剰汚泥１７“とじて汚泥脱水工程（図示せず）に供給さ
れて脱水処分されろ。On the other hand, most of the sludge separated by the UF membrane separating unit [15] is circulated to the storage tank 11 as circulating sludge 17', and the rest is recycled as surplus sludge 17' and supplied to a sludge dewatering process (not shown). Be dehydrated.
なお、実施例フは無機凝集剤等の薬品を第２の生物処理
槽（生物処理槽７）から流出する活性汚泥スラリーに添
加した例を示したが、活性汚泥スラリーを固液分離して
得られた分離水に添加して処理してもよい。In addition, although Example F shows an example in which chemicals such as an inorganic flocculant were added to the activated sludge slurry flowing out from the second biological treatment tank (biological treatment tank 7), the activated sludge slurry obtained by solid-liquid separation was It may be added to the separated water for treatment.
本発明の処理装置は次のような効果を有する。 The processing device of the present invention has the following effects.
■ 第１の生物処理槽に続いて活性汚泥を返送するため
のＵＦ膜分離装置を設ける必要がないため、運転経費、
設備費を従来装置に比べ大きく節減！きる。■ Since there is no need to install a UF membrane separation device to return activated sludge following the first biological treatment tank, operating costs and
Significant savings in equipment costs compared to conventional equipment! Wear.
■ 活性汚泥を第１の生物処理槽に返送するための新装
置として活性汚泥に高分子凝集剤を添加してスクリーン
分離するという手段を取るために活性汚泥分離用の動力
が著しく少なくなる。(2) Since the new device for returning activated sludge to the first biological treatment tank involves adding a polymer flocculant to the activated sludge and performing screen separation, the power required to separate the activated sludge is significantly reduced.
■ 返送汚泥用のスクリーン分離装置などからの分離液
と第１の生物処理槽から流出する活性汚泥スラリーとの
混合液を第２の生物処理槽に導びくようにしており、こ
の槽へ雑排水を供給して処理するようにできるので、第
１の生物処理槽へ雑排水を入れる必要がなくなり、第１
の生物処理槽で雑排水の混入による水温とＭＬＳ Ｓの
低下を防ぐことができ、それにより効率のよい硝化、脱
窒素処理が行える。■ The mixed liquid of the separated liquid from the screen separation device for returned sludge and the activated sludge slurry flowing out from the first biological treatment tank is led to the second biological treatment tank, and gray water is transferred to this tank. Since it is possible to supply and treat gray water, there is no need to put gray water into the first biological treatment tank.
The biological treatment tank prevents the drop in water temperature and MLSS due to the contamination of gray water, thereby allowing efficient nitrification and denitrification treatment.
第１図は、本発明の処理装置の概要図１あり。
第２図は従来のし尿処理装置の概要図１ある。
１・・・し尿 ２・・・第１の生物処理槽
６・・・活性汚泥スラリー ７・・・第２の生物処理槽
１１・・・貯槽 １２・・・無機凝集剤１５
・・・ＵＰ膜分離装ｆｒｔ １７・・・分離汚泥２１
・・・スクリーン分離装置 ２２・・・分離フロック
２３・・・分離液
（は力′ｈ５名）
！ ！
一：４．．ｌいにFIG. 1 is a schematic diagram 1 of a processing apparatus of the present invention. FIG. 2 is a schematic diagram 1 of a conventional human waste processing apparatus. 1... Human waste 2... First biological treatment tank 6... Activated sludge slurry 7... Second biological treatment tank 11... Storage tank 12... Inorganic flocculant 15
...UP membrane separator frt 17...Separated sludge 21
... Screen separation device 22 ... Separation floc 23 ... Separation liquid (5 people)! ! 1:4. ．． lini
Claims (1)
処理槽を設け、また前記生物処理槽から流出する活性汚
泥スラリーを生物処理する第２の生物処理槽を設けると
共に、第１の生物処理槽内にある、もしくは同槽から流
出する活性汚泥スラリーの一部に高分子凝集剤を添加し
、生成フロツクをスクリーン分離する分離装置を設け、
前記分離装置からの分離汚泥を第１の生物処理槽へ返送
する系路と前記分離装置からの分離液を第２の生物処理
槽に供給する系路を設け、第２の生物処理槽からの流出
液に無機系凝集剤を添加して凝集分離する固液分離装置
を設けたことを特徴とするし尿系汚水の処理装置。A first biological treatment tank is provided for biologically nitrifying and denitrifying human waste water, and a second biological treatment tank is provided for biologically treating activated sludge slurry flowing out from the biological treatment tank. A polymer flocculant is added to a portion of the activated sludge slurry in or flowing out from the biological treatment tank, and a separation device is installed to screen and separate the generated flocs.
A system line for returning the separated sludge from the separation device to the first biological treatment tank and a system path for supplying the separated liquid from the separation device to the second biological treatment tank are provided, A treatment device for night soil wastewater, characterized in that it is equipped with a solid-liquid separator that adds an inorganic flocculant to the effluent to perform flocculation and separation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63159417A JPH0649199B2 (en) | 1988-06-29 | 1988-06-29 | Human waste system treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63159417A JPH0649199B2 (en) | 1988-06-29 | 1988-06-29 | Human waste system treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH029497A true JPH029497A (en) | 1990-01-12 |
| JPH0649199B2 JPH0649199B2 (en) | 1994-06-29 |
Family
ID=15693292
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63159417A Expired - Lifetime JPH0649199B2 (en) | 1988-06-29 | 1988-06-29 | Human waste system treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0649199B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03275197A (en) * | 1990-03-23 | 1991-12-05 | Ebara Infilco Co Ltd | Treatment of night soil type sewage |
| JPH044098A (en) * | 1990-04-18 | 1992-01-08 | Ebara Infilco Co Ltd | Treatment of night soil-based sewage |
| KR100383385B1 (en) * | 2000-12-08 | 2003-05-12 | 현대건설주식회사 | Apparatus for filtering water in a membraned-combining type |
| KR100402556B1 (en) * | 2001-08-29 | 2003-10-17 | 지은상 | Water treatment method for using membrane separation device |
| JP2009241052A (en) * | 2008-03-10 | 2009-10-22 | Sumiju Kankyo Engineering Kk | Biological wastewater treatment method and biological wastewater treatment apparatus |
-
1988
- 1988-06-29 JP JP63159417A patent/JPH0649199B2/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03275197A (en) * | 1990-03-23 | 1991-12-05 | Ebara Infilco Co Ltd | Treatment of night soil type sewage |
| JPH044098A (en) * | 1990-04-18 | 1992-01-08 | Ebara Infilco Co Ltd | Treatment of night soil-based sewage |
| KR100383385B1 (en) * | 2000-12-08 | 2003-05-12 | 현대건설주식회사 | Apparatus for filtering water in a membraned-combining type |
| KR100402556B1 (en) * | 2001-08-29 | 2003-10-17 | 지은상 | Water treatment method for using membrane separation device |
| JP2009241052A (en) * | 2008-03-10 | 2009-10-22 | Sumiju Kankyo Engineering Kk | Biological wastewater treatment method and biological wastewater treatment apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0649199B2 (en) | 1994-06-29 |
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