JPH0118795B2 - - Google Patents

Info

Publication number
JPH0118795B2
JPH0118795B2 JP60030701A JP3070185A JPH0118795B2 JP H0118795 B2 JPH0118795 B2 JP H0118795B2 JP 60030701 A JP60030701 A JP 60030701A JP 3070185 A JP3070185 A JP 3070185A JP H0118795 B2 JPH0118795 B2 JP H0118795B2
Authority
JP
Japan
Prior art keywords
stage
tank
aeration
filter bed
biological
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.)
Expired
Application number
JP60030701A
Other languages
Japanese (ja)
Other versions
JPS60241994A (en
Inventor
Beenke Booto
Fuiruku Uorufugangu
Hiberun Kaaru
Katsumi Nomura
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of JPS60241994A publication Critical patent/JPS60241994A/en
Publication of JPH0118795B2 publication Critical patent/JPH0118795B2/ja
Granted legal-status Critical Current

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Classifications

    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/121—Multistep treatment
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/04—Aerobic processes using trickle filters
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • 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

  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biological Treatment Of Waste Water (AREA)
  • Activated Sludge Processes (AREA)

Description

【発明の詳細な説明】 発明の技術分野 本発明は、処理施設中に、汚泥物質の乾燥状態
での１Kgあたり１日に負荷されるBOD量で表さ
れるBOD−MLSS負荷が、２KgBOD5／Kg・
MLSS／日（MLSSは以下単にSSとも表示する）
以上で動作する第一生物段用の曝気槽、この曝気
槽の汚泥を初期馴養期に基質呼吸状態に保つ程度
に余剰汚泥を引抜くため曝気槽の後に接続された
最終沈澱池、および最終沈澱池から流出した水を
導入する第２の好気性生物段が設けられている。
下水、とくに都市下水の２段生物処理方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION Technical Field of the Invention The present invention provides that the BOD-MLSS load, expressed as the amount of BOD loaded per day per 1 kg of dry sludge material, in a treatment facility is 2 Kg BOD 5 / Kg·
MLSS/day (MLSS is also simply referred to as SS below)
An aeration tank for the first biological stage that operates as above, a final settling tank connected after the aeration tank to draw out excess sludge to the extent that the sludge in this aeration tank is kept in a substrate respiration state during the initial acclimatization period, and a final settling tank. A second aerobic biological stage is provided which introduces water runoff from the pond.
The present invention relates to a two-stage biological treatment method for sewage, especially urban sewage.

このような処理方法においては、１段目の生物
学的処理段は吸着段として働く。吸着段は、汚濁
物が大部分吸着（反応）によつて微生物に固着さ
れ、その後余剰汚液とともに排除される。近代的
な活性汚泥段である。さらに、活性汚泥段（＝一
段目）は低負荷ではなくて、充分に負荷を与えら
れた段であつて、すなわち好気性または通性嫌気
性で運転されることが重要である。曝気槽の汚泥
は基質呼吸を用いた初期馴養期状態に保たれなけ
ればならない。言いかえれば、吸着段では、栄養
に対して少ない含有量のバクテリアの生物体量の
状態を得ることによつて非常に大きい生命活動力
つまり非常に高い全体合成速度を持つ低位のバク
テリアだけが生息可能である。そこで下水中の汚
濁物の大部分は呼吸によつて除去されるのではな
く、吸着的に（生物体に）固着され、絶えずくり
返される汚泥増殖（すなわち余剰汚泥）として
（水）処理システムから排除される。それゆえＡ
段（吸着段）は非常に少ないエネルギー消費量で
済む。この一段目（吸着段）での除去率は生物学
的な負荷量（BOD5量として）約50〜60％であ
る。 In such a treatment method, the first biological treatment stage acts as an adsorption stage. In the adsorption stage, most of the pollutants are fixed to microorganisms by adsorption (reaction), and then removed together with excess waste liquid. It is a modern activated sludge stage. Furthermore, it is important that the activated sludge stage (=first stage) is not a lightly loaded stage, but a fully loaded stage, ie operated aerobically or facultatively anaerobically. The sludge in the aeration tank must be maintained in an initial acclimatization state using substrate respiration. In other words, in the adsorption stage, by obtaining a state of low bacterial biomass relative to the nutrients, only low-order bacteria with a very high vitality and thus a very high overall synthesis rate are inhabited. It is possible. Therefore, most of the pollutants in sewage are not removed by respiration, but are adsorbed (on living organisms) and leave the (water) treatment system as constantly repeated sludge growth (i.e., surplus sludge). be excluded. Therefore A
The stage (adsorption stage) consumes very little energy. The removal rate in this first stage (adsorption stage) is about 50 to 60% of the biological load (as BOD 5 amount).

従来技術 周知の処理方法（DE特許26 40 875）によれ
ば、曝気槽は比較的長い滞留時間で運転される。
従つてそれにみ合う構造とそれにみ合う大きな曝
気槽つまり広大な土地を必要とする。２段目の生
物学的処理段は周知の処理方法では、これも曝気
槽を用いて運転される。周知の方法では、各々の
処理段は、一段目の生物学的処理段ではBOD−
SS負荷が少なくとも２KgBOD5／KgSS・日で運
転され、中間沈殿池（＝最終沈殿池）から引き抜
かれる余剰汚泥の量によつて、一段目の曝気槽を
基質呼吸のある初期馴養期状態に保ち、（一段目
と２段目との）厳密な生物相の分離のために２段
目の活性汚泥処理段は考慮され、究極的には、
BOD−SS負荷0.15KgBOD5／KgSS・日で運転さ
れる２段目の活性汚泥処理段から出る余剰汚泥
は、（一段目に）返送されることなく系外に排出
される。以上のことはすでに確証されたが、しか
しそれに見合う建設出費特に（２段目の）曝気槽
と最終沈殿池に大きな敷地を必要とする。PRIOR ART According to the known treatment method (DE patent 26 40 875), the aeration tank is operated with relatively long residence times.
Therefore, it requires a suitable structure and a correspondingly large aeration tank, which means a large area of land. In known treatment methods, the second biological treatment stage is also operated using an aeration tank. In the known method, each treatment stage has a BOD-
The SS load is operated at at least 2KgBOD 5 /KgSS・day, and the first stage aeration tank is maintained in an initial acclimatization state with substrate respiration by the amount of excess sludge drawn from the intermediate settling tank (= final settling tank). , a second activated sludge treatment stage is considered for strict biota separation (between the first and second stage), and ultimately,
Excess sludge from the second activated sludge treatment stage, which is operated at a BOD-SS load of 0.15KgBOD 5 /KgSS/day, is discharged outside the system without being returned (to the first stage). This has already been established, but the construction costs are commensurate with the large area required, especially for the (second stage) aeration tank and the final settling tank.

発明の目的 本発明の課題は与えられた量の下水に対し、同
じ処理成績、同じ処理効率およびエネルギー消費
でかなり少ない建設出費特に少ない敷地でこの方
法が運転可能なように初めに述べた方法を改善す
ることにある。OBJECTS OF THE INVENTION The object of the invention is to develop the method mentioned at the outset in such a way that for a given amount of sewage, the method can be operated with the same treatment performance, the same treatment efficiency and energy consumption, with considerably less construction outlay, especially on a smaller site. It's about improving.

発明の構成 この課題を解決するため本発明は次のことを示
している。すなわち45分またはそれ以下の滞留時
間で曝気槽を運転し、かつ曝気槽から最終沈殿池
を介して、１m3あたり0.5ないし1.5重量％の活性
汚泥を第２生物段に移し、また第２生物段とし
て、上部に生物学的に活性の有孔性層と下部に
砂層を備えたフイルタベツドを使用し、しかもフ
イルタベツドから流出した水の一部を返送し、返
送割合も含めた事実上の速を５ｍ／ｈないし20
ｍ／ｈの範囲にし、フイルタベツドにおいて１m3
および１日あたり６ないし18KgBOD5の容積負荷
で運転し、また生物学的に活性の有孔性層は、
100cmの層厚を有し、砂層は少なくとも75cmの厚
さを有し、砂粒径は0.7ないし1.2mmである。Structure of the Invention In order to solve this problem, the present invention shows the following. That is, the aeration tank is operated with a residence time of 45 minutes or less, and 0.5 to 1.5% by weight of activated sludge per m 3 is transferred from the aeration tank to the second biological stage via the final settling tank, and the second biological stage is As a stage, a filter bed with a biologically active porous layer on the top and a sand layer on the bottom is used, and a part of the water runoff from the filter bed is returned, reducing the actual speed including the return rate. 5m/h to 20
m/h range, 1m3 in filter bed
and operating at a volumetric load of 6 to 18 Kg BOD 5 per day, and a biologically active porous layer.
The layer thickness is 100 cm, the sand layer is at least 75 cm thick, and the sand grain size is 0.7 to 1.2 mm.

なかんずく曝気槽はBOD−SS負荷２Kg／
BOD5／Kg・MLSS／日及びMLSS…1.0〜2.5
ｇ／ｌなかでも2.0ｇ／ｌで運転され、滞留時間
も45分よりずつと短くともよい。曝気槽（一段
目）の溶存酸素濃度は0.5〜１mg／ｌで運転され
るべきである。本発明は、このような方法におい
て前記の運転パラメータを保つことによつて（一
段目曝気槽の）滞留時間が高々45分またはそれ以
下であるように曝気槽を運転できるという知識を
前提とする。これによりこの曝気槽においてすで
に敷地を縮少することができるのである。２段目
の生物学的処理段は過層段である。層は周知
の方法の２段目の活性汚泥処理段よりもかなり少
ない用地で済む。曝気槽を出て、最終沈殿池（中
間沈殿池）を通り、２段目の活性汚泥段に流入す
る水は、このような運転をした場合、一段目の生
物処理段の生物体を連行するが、この生物体はも
し、その量が一段目の生物処理段中に１m3当り
0.5〜1.5重量％の活性汚泥の割合に保たれ、さら
に加えて、層が前記の処置により運転されるな
らば決して害がない。２段目に流入した水のそれ
以後の必要とされる浄化については、物理的でし
かも生物学的な濾過手段を有する高速濾過装置に
よつて行われる。両方の作用を組合わせると、こ
の２段目も、高い生物学的負荷（BOD負荷）で
あるにもかかわらず、非常に低い放流水質汚濁濃
度を得ることができる。過段での運転法は吸着
段の出口の水質によつて決定される。層生物を
ずつと維持するためには有孔性の材と酸素の供
給が必要である。それにより沈殿しやすい固着生
物体によつて生物膜が形成されるのである。 Above all, the aeration tank has a BOD-SS load of 2 kg/
BOD 5 /Kg・MLSS/day and MLSS…1.0~2.5
It may be operated at 2.0 g/l, and the residence time may be as short as 45 minutes. The aeration tank (first stage) should be operated with a dissolved oxygen concentration of 0.5-1 mg/l. The invention is premised on the knowledge that in such a method, by maintaining the above-mentioned operating parameters, the aeration tank can be operated such that the residence time (in the first stage aeration tank) is at most 45 minutes or less. . This makes it possible to already reduce the area required for this aeration tank. The second biological treatment stage is a superlayer stage. The layer requires significantly less land than the second activated sludge treatment stage of known processes. When operated in this way, the water that leaves the aeration tank, passes through the final sedimentation tank (intermediate sedimentation tank), and flows into the second activated sludge stage will entrain the living organisms from the first biological treatment stage. However, if the amount of this organism is per 1m3 during the first biological treatment stage,
If the proportion of activated sludge is kept at 0.5-1.5% by weight and, in addition, the bed is operated according to the above-mentioned procedure, it will not cause any harm. The subsequent necessary purification of the water entering the second stage is carried out by a high-speed filtration device having both physical and biological filtration means. By combining both actions, this second stage can also achieve a very low effluent water pollution concentration despite a high biological load (BOD load). The mode of operation in stages is determined by the quality of the water at the outlet of the adsorption stage. Porous materials and oxygen supply are necessary to maintain the layered organisms. As a result, biofilms are formed by sessile organisms that tend to settle.

一段目の最高負荷活性汚泥段または吸着段（既
述）から生物フロツクを作る習性のないバクテリ
アが流れて来るので（過段では）生物学的に活
発な層の下に粒径の小さい、ほどよい能力を持
つた砂層を配置している。層が好気的に働らく
よう正しく保たれるためには、過される水が少
なくとも約６mg／ｌの溶存酸素濃度を持ち、それ
によつて生物学的に活発な有孔性の床全体が好
気的に働くよう満足されていなければならないこ
とは明らかである。そのためには最終沈殿池から
流出して来る水は、床段階に入る前に曝気槽で
酸素および／または空気で曝気されなければなら
ない。過段から流出した水が返送されて運転を
している場合には、曝気の前で最終沈殿池から流
出した水は返送された過水と混合されなければ
ならない。そうすることによつて充分な水量とそ
れによる酸素が床内に入るのである。一般的に
は最大３倍量の返送で運転される。また晴天時に
は実質的な過速度は返送分も含めて5.0ｍ／ｈ
から20.0ｍ／ｈまでである。雨水が流入する雨天
時に運転する場合は最大実質過速度20ｍ／ｈで
運転し、この速度を越えないよう過水返送割合
が調節される。また曝気槽には予備浄化なしで下
水を投入することができる。 Bacteria that do not have the habit of forming biological flocs flow from the first highest load activated sludge stage or adsorption stage (as described above), so bacteria with small particle size are deposited under the biologically active layer (in upper stages). A sand layer with good properties is placed. In order for the bed to work properly aerobically, the water being filtered must have a dissolved oxygen concentration of at least about 6 mg/l, so that the entire biologically active porous bed is It is clear that it must be satisfied to work aerobically. To this end, the water leaving the final settling basin must be aerated with oxygen and/or air in an aeration tank before entering the bed stage. If the operation is carried out with water flowing back from the overstage, the water flowing out from the final settling basin must be mixed with the returned overwater before aeration. This allows sufficient water and therefore oxygen to enter the bed. Generally, it is operated with a maximum of three times the amount returned. Also, on clear days, the actual overspeed is 5.0m/h including the return speed.
to 20.0m/h. When operating in rainy weather when rainwater flows in, the system operates at a maximum effective overspeed of 20 m/h, and the excess water return ratio is adjusted so as not to exceed this speed. In addition, sewage can be poured into the aeration tank without preliminary purification.

達成された効果は要約すると、与えられた下水
量に対して、同じような処理成績、同じようなエ
ネルギー消費および少なくとも同程度の処理効率
で、しかも公知の方法よりかなり少ない建設費用
特に用地で運転できることである。このことは、
処理成績と処理効率に関して、驚異的である。な
ぜなら世に優勢な教えによれば放流水質基準を満
足するためにはBOD−SS負荷が0.15KgBOD5／
Kg・MLSS／日の低い汚泥負荷で運転しなければ
ならなかつたからであつた。本発明はこれらの経
験から逸脱しており、最終段には低い負荷の処理
段を必要とせず、しかもそれにもかかわらず要求
される放流水質基準を達成できるのである。吸着
段も過段も本発明の範囲においては高負荷で運
転されている。吸着段はBOD容積負荷が例えば
10KgBOD5／m3・日、過段は同じく６〜18Kg
BOD5／m3・日である。実験によれば（一段目
の）BOD−MLSS負荷３〜４KgBOD5／Kg・
MLSS／日のとき、過段の処理効率は200％の
返送のときにCODcr60％〜62％BOD580％である。
本発明に従つて吸着段と活発に働く過段とを組
み合わせた場合、合計の除去成績はCODcrη＝82
％、BOD5η＝95％である。 The effects achieved can be summarized as follows: for a given amount of sewage, similar treatment performance, similar energy consumption and at least the same treatment efficiency, but with considerably lower construction costs than known methods, especially when operating on site. It is possible. This means that
It is amazing in terms of processing results and processing efficiency. This is because, according to the prevailing teaching, in order to satisfy the discharge water quality standards, the BOD-SS load must be 0.15KgBOD 5 /
This was because it had to be operated at a low sludge load in kg/MLSS/day. The present invention departs from these experiences in that it does not require a final, low-load treatment stage, yet still achieves the required effluent quality standards. Both the adsorption stages and the superstages are operated at high loads within the scope of the invention. In the adsorption stage, the BOD volumetric load is e.g.
10KgBOD 5 /m 3・day, same 6-18Kg for overboard
BOD 5 / m3・day. According to experiments, the BOD-MLSS load (first stage) is 3~4KgBOD 5 /Kg・
At MLSS/day, the over-stage processing efficiency is COD cr 60%-62% BOD 5 80% at 200% return.
When combining an adsorption stage and an active stage according to the present invention, the total removal performance is COD cr η = 82
%, BOD 5 η = 95%.

実施例の説明 以下は本発明を処理方法のフローシートをもと
に解説したものである。その次に実施例が示して
ある。DESCRIPTION OF EXAMPLES The present invention is explained below based on a flow sheet of a treatment method. Examples are then presented.

この処理方法のフローシート図は下水の処理と
くに都市下水の処理のための施設を示す。このフ
ローシートではまず曝気槽１、最終沈殿池２、
過床段３が示されている。下水はまず本実施例で
は最初沈殿池を通すことなく４のところで曝気槽
１に投入される。最終沈殿池からは５を通じ余剰
汚泥を引き抜くことが可能である。最終沈殿池を
出た水は６を通り、過床段３へ投入され過床
段３で物理的に過される。曝気槽１は吸着段
（以後Ａ段と呼ぶ）として運転される。過床段
３は物理的な過に加えて曝気した好気性生物段
として運転される。そのために最終沈殿池２と
過床段３の間に曝気装置７が配置され、これによ
つて最終沈殿池から流出した水に酸素が加えられ
る。過床段３ないし８から流出した水は返送装
置９によつて一部最終沈殿池の段で最終沈殿池か
ら流出した水と１０のところで再び混合される。
このとき返送装置９は最大３倍の返送率まで行な
えるよう考慮されている。もちろんＡ段の前に粗
目スクリーン、沈砂池細目スクリーンを配置して
もかまわない。 The flow sheet diagram of this treatment method shows facilities for the treatment of sewage, especially urban sewage. In this flow sheet, first, aeration tank 1, final settling tank 2,
Overbed tier 3 is shown. In this embodiment, the sewage is first introduced into the aeration tank 1 at point 4 without passing through the settling tank. Excess sludge can be drawn out from the final settling tank through 5. The water leaving the final settling tank passes through 6 and is input into the overbed stage 3 where it is physically filtered. The aeration tank 1 is operated as an adsorption stage (hereinafter referred to as A stage). Overbed stage 3 is operated as an aerobic biological stage with physical overflow as well as aeration. For this purpose, an aeration device 7 is arranged between the final settling basin 2 and the overbed stage 3, by means of which oxygen is added to the water leaving the final settling basin. The water flowing out from the overbed stages 3 to 8 is mixed again at 10 with the water flowing out from the final settling basin, in part, by means of a return device 9 in the stage of the final settling basin.
At this time, the return device 9 is designed to be able to perform a return rate of up to three times. Of course, a coarse screen or a fine settling basin screen may be placed in front of the A stage.

（好気性の範囲で生物学的処理を行なう有孔性
の過床は周知であるが（VSA−フアツハター
グング1982グロス他による。“シユペツイーレ、
アスペクテ、デア、フイルトレーシヨズテクニー
ク…”）、しかしながら周知の方法では本発明にお
ける課題を満足するためには何も貢献していな
い。） 実施例 人口100000人当量の例では次のようなデーター
が有効である。 (Although porous overbeds with biological treatment in the aerobic range are well known (VSA-Vasshattagung 1982 Gross et al.
However, the well-known methods do not contribute anything to satisfying the object of the present invention.) Example In an example with a population of 100,000 person equivalents, the following data is used. is valid.

１日水量（下水量） Qd＝33000m3／日 時間最大汚水負荷量（晴天時）
Qtr＝2000m3／日 時間最大汚水量（雨天時） Qr＝3500m3／日 生物学的負荷Ｂ＝100000人×0.060BODKg／人
＝6000KgBOD5／日 平均流入下水濃度
So＝約180mg／ｌ（BOD5として） 各々の建設部分は次のように設定される。 Daily water volume (sewage volume) Qd = 33000m 3 /day Maximum hourly sewage load (when it is sunny)
Qtr= 2000m3 /day Maximum hourly sewage volume (in rainy weather) Qr= 3500m3 /day Biological load B=100000 people×0.060BODKg/person=6000KgBOD 5 /day Average inflow sewage concentration
So=approximately 180 mg/l (as BOD 5 ) Each construction section is set as follows.

１ 粗目スクリーン 標準型 ２ 沈砂池 標準型 曝気または無曝気 ３ 細目スクリーン 標準型 ４ Ａ段 生物学的負荷 BB＝6000KgBOD5／日 BOD容積負荷 BR＝８KgBOD5／m3・日 曝気槽生物体量（＝MLSS） TSR＝２Kg
TS／m3（＝2000mg／ｌ） 汚泥負荷（BOD−SS負荷） BTS＝８／２＝４Kg BOD5／KgSS・日 容 積 VA＝6000÷８＝750m3 滞留時間 TR＝750／2000×60＝22.5min 曝気槽溶存酸素 1.0ｇO2／ｌのときのBOD5
除去率約55％ ５ 最終沈殿池 Ａ段の汚泥は沈降性が非常に良い、従つて晴天
時の水量負荷の多い時間帯に滞留時間が2.5時間
あるように設定する。雨天時の沈殿時間は2.5×
2000／3500＝1.43時間となる。最終沈殿池で沈降した 汚泥は再びＡ段へ返送されるように集泥装置を組
み、返送先は細目スクリーンの前になるようにす
る。Ａ段と最終沈殿池を通つた処理水は SA＝（１−0.55）×180＝81mg／lBOD5となる。1 Coarse screen Standard type 2 Sediment basin Standard type Aeration or non-aeration 3 Fine screen Standard type 4 Stage A Biological load B B = 6000KgBOD 5 /day BOD volumetric load B R = 8KgBOD 5 /m 3・day Aeration tank biological body Quantity (=MLSS) TS R = 2Kg
TS/m 3 (=2000mg/l) Sludge load (BOD-SS load) B TS = 8/2 = 4Kg BOD 5 /KgSS・day Volume V A = 6000÷8 = 750m 3 Retention time T R = 750/ 2000×60=22.5min BOD 5 when dissolved oxygen in aeration tank is 1.0gO 2 /l
Removal rate of approximately 55% 5. Final settling tank The sludge in stage A has very good settling properties, so it is set so that it has a retention time of 2.5 hours during sunny days when the water load is high. Sedimentation time in rainy weather is 2.5×
2000/3500=1.43 hours. A sludge collector is installed so that the sludge settled in the final settling tank is returned to stage A, and the return destination is in front of the fine screen. The treated water that has passed through Stage A and the final settling tank is S A = (1-0.55) x 180 = 81 mg/l BOD 5 .

６ 過段 ６，１ 曝気槽 滞留時間は（過との）３倍の返送を含めて日
平均で少なくとも5minとする。6 Passage stage 6, 1 Aeration tank Residence time shall be at least 5 min on average per day, including 3 times return (with respect to filtration).

容積VBel＝（１＋３）×33000／24.60×５＝458m3 ６，２ 過床 施設流入水あたりの平均過速度 VF＝５
ｍ／ｈ 平均流入水量に対する最大返送率 RV＝300％ 最大実質過速度 VF＝20ｍ／ｈ 必要濾過床面積 FF＝33000／24×5.0＝275m2 10個に分け各40m2の表面積 層上部は粒径 2.5〜3.5mmの軽石 層厚は Tpb＝1.10ｍ 層下部は粒径 0.7〜1.2mmの砂 層厚は Tu＝0.90ｍ 過塔に対する生物学的負荷 BF＝6000×（１
−0.55）＝2700KgBOD5／日 生物学的に活発な層に対する BOD容積負荷 BRF＝2700／275×1.0＝9.8KgBOD5／ m3・日 過部でのBOD5除去率 ηF＝88％ 過流出水 SF＝約10mg／lBOD5 ６，３ 逆洗水 過床の再生は一日に一回空気と水で行なう。
この水は過水を一時留めたものを使う。この洗
浄水用の池は過床一単位分の量で充分である。
15分の洗浄、最大逆洗速度50ｍ／ｈとすれば洗浄
水用池の面積は Ｖ＝27.5×50×15／60＝344m3 ６，４ 逆洗汚泥貯留槽 逆洗汚泥はまた500m3の大きさの池にに集めら
れる。20分の沈殿時間ののち、沈殿した汚泥は汚
泥処理の方へポンプ移送され、これから出る少量
の汚水はＡ段の流入へ戻される。ポンプは344
m3／ｈの能力とする、これにより約1.5時間後に
は次の過床の逆洗ができるようにする。これに
より水量負荷の高い日中10時間の間全く逆洗をし
なくても良いようにする。 Volume V Bel = (1 + 3) × 33000 / 24.60 × 5 = 458 m 3 6, 2 Overbed Average overvelocity per facility inflow V F = 5
m/h Maximum return rate for average inflow water volume RV = 300% Maximum effective overvelocity V F = 20 m/h Required filtration bed area F F = 33000/24 x 5.0 = 275 m 2 Divided into 10 pieces, each 40 m 2 Surface area Top of layer is pumice with a grain size of 2.5 to 3.5 mm The layer thickness is T pb = 1.10 m The lower part of the layer is sand with a grain size of 0.7 to 1.2 mm The layer thickness is T u = 0.90 m Biological load on the tower B F = 6000 x (1
−0.55) = 2700KgBOD 5 / day BOD volumetric load on biologically active layer B RF = 2700/275×1.0 = 9.8KgBOD 5 / m 3 ·day BOD 5 removal rate η F = 88% Effluent S F = approx. 10 mg/l BOD 5 6.3 Backwash water Regeneration of the overbed is performed once a day with air and water.
Use water that has been temporarily stagnated. The amount of this wash water pond is sufficient for one unit of overbed.
If the washing time is 15 minutes and the maximum backwashing speed is 50m/h, the area of the washing water pond is V = 27.5 x 50 x 15/60 = 344m 3 6,4 Backwash sludge storage tank Backwash sludge is also 500m 3 They are collected in ponds of the same size. After a settling time of 20 minutes, the settled sludge is pumped to the sludge treatment and a small amount of sewage from this is returned to the stage A inlet. Pump is 344
m 3 /h, so that the next overbed can be backwashed after about 1.5 hours. This eliminates the need for backwashing at all during the 10 hours during the day when the water load is high.

７ 汚泥処理 汚泥処理は標準法による消化タンク、場合によ
つては濃縮装置、汚泥脱水によつて行われる。7 Sludge treatment Sludge treatment is carried out by standard methods in digestion tanks, possibly thickeners, and sludge dewatering.

利点の要約 最高負荷活性汚泥段と生物学的に活発な過と
の組み合わせは活性汚泥処理法による標準下水処
理法に比べ次のような利点がある。Summary of Advantages The combination of a full-load activated sludge stage and a biologically active filtration system has the following advantages over standard wastewater treatment methods using activated sludge treatment methods:

極めて少ない用地面積：BOD−SS負荷0.3Kg
BOD5／KgSS・日の標準活性汚泥法に比べドイツ
の設計指針によつても国際的な設計指針によつて
も50％以下の用地面積で済む。 Extremely small land area: BOD-SS load 0.3Kg
Compared to the standard activated sludge process of BOD 5 /KgSS/day, it requires less than 50% of the land area according to both German and international design guidelines.

下水中の有機物を分解するのに必要な酸素量を
減らすことができる、理由1A曝気槽では（生物
学的に）低位のバクテリアが高い同化速度をもつ
て活動している。そのほか、処理反応は吸着過程
を主としている。理由２その後につづく過段で
は直接的な生物学的除去の他に物理的な浄化機能
が高い割合である。浮遊物質とコロイド状物質は
材の生物膜によつて非常に良好に補促される。 The amount of oxygen needed to decompose organic matter in sewage can be reduced because: 1A In the aeration tank, (biologically) lower level bacteria are active with a high assimilation rate. In addition, the processing reactions mainly involve adsorption processes. Reason 2 The subsequent stages have a high proportion of physical purification functions in addition to direct biological removal. Suspended and colloidal substances are very well supported by the biofilm of the wood.

バルキング（膨化）汚泥の存在はありえない。
というのも最高負荷で運転されている曝気槽は原
則的に非常に沈降性の高い汚泥を生産し、それに
つづく過段も固定床反応槽としてそのシステム
からしてこれもバルキングの発生はないからであ
る。バルキング汚泥の発生と、それに伴なつて避
け得るはずの放流水質基準オーバーの危険はここ
に紹介した組み合わせで排除される。 The existence of bulking sludge is impossible.
This is because the aeration tank operated at maximum load basically produces sludge with very high settling properties, and the subsequent stage is also a fixed bed reaction tank, which does not cause bulking due to its system. It is. The combination introduced here eliminates the generation of bulking sludge and the associated risk of exceeding the discharge water quality standards, which could have been avoided.

【図面の簡単な説明】[Brief explanation of drawings]

図は、本発明による方法を実施する施設を示す
処理方式図である。 １……曝気槽、２……最終沈殿池、３……過
床段、７……曝気装置。 The figure is a process diagram showing a facility implementing the method according to the invention. 1... Aeration tank, 2... Final settling tank, 3... Overbed stage, 7... Aeration device.

Claims (1)

【特許請求の範囲】 １ 処理施設中において、汚泥物質（乾燥重量）
１Kgあたり、１日に負荷されるBOD量（Kg）で
表されるBOD−MLSS負荷が、２KgBOD5／Kg・
MLSS／日以上で動作する第１の生物段用の第１
の曝気槽が設けられており、この第１の生物段
は、0.5〜１mg／ｌの酸素含有量で、45分または、
それ以下の滞留時間で動作し、第１の曝気槽の後
には、これに接続する最終沈澱池が設けられてお
り、第１の曝気槽の汚泥を初期馴養期に基質呼吸
状態に保つ程度に最終沈澱池から余剰汚泥を引抜
いて吸着段を形成し、かつその後に第２の好気性
生物段が設けられており、最終沈澱池から流出し
た水を第２の好気性生物段に導入する下水、特に
都市下水の２段生物処理方法において、 第２の生物段を、上部に生物学的に活性の有孔
性濾層と、下部に砂層を備えたフイルタベツドと
して形成し、第２の生物段の前に曝気段が接続さ
れており、曝気槽から最終沈澱池を介して、１m3
あたり0.5〜1.5重量％の活性汚泥を第２の生物段
に移し、しかも曝気段を介してフイルタベツドへ
の流入水が、その入口において少なくとも６mg／
ｌの溶存酸素濃度であるようにし、フイルタベツ
ドから流出する水の一部を曝気段の前に返送し、
フイルタベツドにおける濾速を、前記返送量も含
めて５ｍ／時〜20ｍ／時の範囲にし、さらにフイ
ルタベツドにおいて１m3あたり６〜18KgBOD5の
容積負荷を維持し、かつ生物学的に活性な有孔性
濾層は少なくとも100cmの層厚を有し、砂層は少
なくとも75cmの厚さを有し、砂粒径は0.7mm〜1.2
mmであることを特徴とする、下水、とくに都市下
水の２段生物処理方法。 ２ 最終沈澱池から流出した水を、フイルタベツ
ドに入る前に、曝気段において酸素または空気で
曝気する、特許請求の範囲第１項に記載の方法。 ３ フイルタベツドから流出した水の返送分を、
最終沈澱池から流出した水の曝気の前に、この水
に再び混合する、特許請求の範囲第２項に記載の
方法。 ４ フイルタベツドから流出した水を、最終沈澱
池から流出した水の３倍までの返送率で返送す
る、特許請求の範囲第３項に記載の方法。 ５ 雨水が流入する場合、フイルタベツドを20
ｍ／時の濾過速度で運転し、かつこの速度を返送
率を変えることによつて調節する、特許請求の範
囲第１〜第４項の一つに記載の方法。 ６ 予備浄化せずに下水を曝気槽に注入する特許
請求の範囲第１〜第５項の一つに記載の方法。[Scope of Claims] 1. In a treatment facility, sludge material (dry weight)
The BOD-MLSS load expressed as the BOD amount (Kg) loaded per 1Kg per day is 2KgBOD 5 /Kg・
The first for the first biological stage operating at MLSS/day or higher.
This first biological stage is heated for 45 minutes or at an oxygen content of 0.5-1 mg/l.
A final sedimentation tank is installed after the first aeration tank and is connected to the first aeration tank to maintain the sludge in the first aeration tank in a state of substrate respiration during the initial acclimatization period. Excess sludge is drawn out from the final settling tank to form an adsorption stage, and a second aerobic biological stage is provided after that, and the water flowing out from the final settling tank is introduced into the second aerobic biological stage. , especially in a two-stage biological treatment method for urban sewage, in which the second biological stage is formed as a filter bed with a biologically active porous filter layer on top and a sand layer on the bottom; An aeration stage is connected in front of the tank, and from the aeration tank to the final sedimentation tank, 1 m 3
0.5 to 1.5 wt.
1 of the dissolved oxygen concentration, and part of the water flowing out from the filter bed is returned to the front of the aeration stage.
The filtration rate in the filter bed, including the above-mentioned return rate, is in the range of 5 m/h to 20 m/h, and the volume load of the filter bed is maintained in the range of 6 to 18 Kg BOD 5 per m3 , and the pores are biologically active. The filter layer has a layer thickness of at least 100cm, the sand layer has a thickness of at least 75cm, and the sand grain size is 0.7mm~1.2
A two-stage biological treatment method for sewage, especially urban sewage, characterized in that mm. 2. The method according to claim 1, wherein the water flowing out of the final settling basin is aerated with oxygen or air in an aeration stage before entering the filter bed. 3 The amount of water that flows out from the filter bed is returned to
3. A process according to claim 2, wherein the water effluent from the final settling basin is remixed before aeration. 4. The method according to claim 3, wherein the water flowing out from the filter bed is returned at a return rate up to three times that of the water flowing out from the final settling basin. 5 If rainwater flows in, use a filter bed of 20
5. The process as claimed in claim 1, wherein the process is operated at a filtration rate of m/h and this rate is adjusted by varying the return rate. 6. A method according to one of claims 1 to 5, in which sewage is injected into the aeration tank without preliminary purification.
JP60030701A 1984-02-22 1985-02-20 Two-step biological treating method of sewage, particularly,urban sewage Granted JPS60241994A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3406312A DE3406312C2 (en) 1984-02-22 1984-02-22 Process for the two-stage biological purification of wastewater, in particular municipal wastewater
DE3406312.9 1984-02-22

Publications (2)

Publication Number Publication Date
JPS60241994A JPS60241994A (en) 1985-11-30
JPH0118795B2 true JPH0118795B2 (en) 1989-04-07

Family

ID=6228444

Family Applications (1)

Application Number Title Priority Date Filing Date
JP60030701A Granted JPS60241994A (en) 1984-02-22 1985-02-20 Two-step biological treating method of sewage, particularly,urban sewage

Country Status (2)

Country Link
JP (1) JPS60241994A (en)
DE (1) DE3406312C2 (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10127412A1 (en) * 2001-06-06 2003-05-15 Horst Ksienzyk Optimization of biofiltration performance in external or internal filters in purification of still water involves introducing oxygen before or during biofiltration stage

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2803759C3 (en) * 1978-01-28 1983-01-13 Böhnke, Botho, Prof. Dr.-Ing. Two-stage system for the treatment of wastewater according to the activated sludge process
JPS5556892A (en) * 1978-10-21 1980-04-26 Yamazaki Kogyo Kk Treatment method of polluted water
DE3043820A1 (en) * 1980-11-20 1982-06-24 Linde Ag, 6200 Wiesbaden METHOD AND DEVICE FOR BIOLOGICAL WASTE WATER TREATMENT

Also Published As

Publication number Publication date
JPS60241994A (en) 1985-11-30
DE3406312A1 (en) 1985-08-22
DE3406312C2 (en) 1993-12-09

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