JPH0724834B2 - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JPH0724834B2 JPH0724834B2 JP1212191A JP21219189A JPH0724834B2 JP H0724834 B2 JPH0724834 B2 JP H0724834B2 JP 1212191 A JP1212191 A JP 1212191A JP 21219189 A JP21219189 A JP 21219189A JP H0724834 B2 JPH0724834 B2 JP H0724834B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- sludge
- liquid
- concentration
- wastewater treatment
- 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 - Fee Related
Links
Landscapes
- Treatment Of Sludge (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【発明の詳細な説明】 産業上の利用分野 本発明は廃水処理方法に関し、特にし尿や浄化槽汚泥な
どの高濃度汚泥を高負荷脱窒素処理するための廃水処理
方法に関する。TECHNICAL FIELD The present invention relates to a wastewater treatment method, and more particularly to a wastewater treatment method for high-load denitrification treatment of high-concentration sludge such as human waste and septic tank sludge.
従来の技術 第２図は、従来のこの種の高負荷脱窒素処理のための装
置の概略構成を示す。ここで１は硝化・脱窒素槽で、し
尿などの原水２の供給を受けるとともに、その底部に反
応のための空気３が供給されるようになっている。４は
ポンプ５を備えた循環路で、槽内の液の循環のために用
いられる。硝化・脱窒素槽１には、硝酸化槽６、脱窒素
槽７、再曝気槽８および汚泥分離槽９がこの順で接続さ
れている。2. Description of the Related Art FIG. 2 shows a schematic configuration of a conventional apparatus for high load denitrification of this type. Here, 1 is a nitrification / denitrification tank, which is supplied with raw water 2 such as human excrement and at the bottom thereof is supplied with air 3 for reaction. Reference numeral 4 is a circulation path provided with a pump 5 and is used for circulating the liquid in the tank. A nitrification tank 6, a denitrification tank 7, a re-aeration tank 8 and a sludge separation tank 9 are connected in this order to the nitrification / denitrification tank 1.
汚泥分離槽９は液中の固形物を沈降させることによって
この液を濃縮させるもので、濃縮により生じた分離液は
分離液貯槽10に送られるようになっている。また濃縮に
より生じた汚泥は、その一部が返送汚泥11として硝化・
脱窒素槽１へ戻され、かつその残部が余剰汚泥12として
汚泥濃縮貯留槽13へ送られる。14,15はポンプである。The sludge separation tank 9 concentrates the liquid by settling the solid matter in the liquid, and the separated liquid generated by the concentration is sent to the separated liquid storage tank 10. In addition, a part of the sludge generated by the concentration is nitrified as return sludge 11.
It is returned to the denitrification tank 1 and the rest is sent to the sludge concentration storage tank 13 as excess sludge 12. 14 and 15 are pumps.
汚泥濃縮貯留槽13は、後続の脱水機16におけるバッチ処
理に対応できるように余剰汚泥12を一時的に貯留すると
ともに、この余剰汚泥12をさらに沈降により濃縮する。
そして濃縮された汚泥は、ポンプ17によって凝集混和槽
18へ送られる。凝集混和槽18は、モータ19にて駆動され
る攪拌羽根20を有しており、ポンプ21によって送られて
くる凝集剤22と汚泥とを混和して、この汚泥を凝集沈殿
させる。凝集した汚泥はポンプ30によって脱水機16へ送
られ、ここで脱水処理される。脱水により生じたケーキ
は、系外へ排出される。脱水分離液23は分離液貯槽10へ
送られる。The sludge concentration storage tank 13 temporarily stores the excess sludge 12 so as to be able to handle the batch processing in the subsequent dehydrator 16, and further concentrates the excess sludge 12 by sedimentation.
The concentrated sludge is then agglomerated and mixed by the pump 17.
Sent to 18. The coagulation / mixing tank 18 has a stirring blade 20 driven by a motor 19, mixes the coagulant 22 and sludge sent by a pump 21, and coagulates and precipitates this sludge. The coagulated sludge is sent to the dehydrator 16 by the pump 30 and is dehydrated there. The cake produced by dehydration is discharged outside the system. The dehydrated separated liquid 23 is sent to the separated liquid storage tank 10.
分離液貯槽10からの分離液24は、ポンプ25により緩速急
速混和槽26および沈殿槽27へ送られ、ここでCOD処理な
どの高度処理が行われる。沈殿槽27で生じた凝沈汚泥28
は、ポンプ29によって硝酸化槽６へ送られる。The separated liquid 24 from the separated liquid storage tank 10 is sent by the pump 25 to the slow and rapid mixing tank 26 and the precipitation tank 27, where advanced processing such as COD processing is performed. Settled sludge 28 generated in settling tank 27
Is sent to the nitrification tank 6 by a pump 29.
発明が解決しようとする課題 しかし、このような従来のものでは、次に述べるような
問題点がある。SUMMARY OF THE INVENTION However, such a conventional device has the following problems.
（ｉ）汚泥濃縮貯留槽13が嫌気状態になりやすいため、
脱水機16における脱水濾液中のアンモニア性窒素濃度が
上昇し、放流水のトータル窒素濃度が上昇する。(I) Since the sludge thickening storage tank 13 is easily anaerobic,
The concentration of ammonia nitrogen in the dehydrated filtrate in the dehydrator 16 increases, and the total nitrogen concentration of the discharged water increases.
（ii）汚泥分離槽９は重力の作用だけで固形分を沈降さ
せるものであるため、SSの除去が不安定であり、凝集沈
殿の状態が不安定となって放流水質が悪化する。(Ii) Since the sludge separation tank 9 settles solids only by the action of gravity, the removal of SS is unstable, the state of coagulation and sedimentation becomes unstable, and the quality of discharged water deteriorates.
（iii）SS除去を安定したものとするために、汚泥分離
槽９からの分離液のオーバーフローをなくし、余剰汚泥
12を脱水機16にて脱水処理することにより処理水の全量
を得ようとすると、MLSS濃度の調整が困難であるうえ
に、試運転時の立ち上げが困難である。(Iii) In order to stabilize the SS removal, the overflow of the separated liquid from the sludge separation tank 9 is eliminated, and the excess sludge is removed.
If an attempt is made to obtain the total amount of treated water by dehydrating 12 with the dehydrator 16, it will be difficult to adjust the MLSS concentration and also difficult to start up during the trial run.
（iv）汚泥分離槽９での固液分離を安定させるために、
原水２を均等投入する必要がある。そこで本発明はこれ
ら問題点を解消することができる廃水処理方法を提供す
ることを目的とする。(Iv) In order to stabilize the solid-liquid separation in the sludge separation tank 9,
Raw water 2 needs to be evenly added. Therefore, an object of the present invention is to provide a wastewater treatment method capable of solving these problems.
課題を解決するための手段 上記目的を達成するため本発明は、再曝気槽内の液を膜
分離装置により濾過処理可能として、この再曝気槽内の
液を必要に応じて濃縮処理するとともに、この再曝気槽
内の液を、汚泥分離槽および汚泥濃縮貯留槽を通すこと
なしに直接脱水処理するものである。Means for Solving the Problems In order to achieve the above-mentioned object, the present invention allows the liquid in the re-aeration tank to be subjected to a filtration treatment by a membrane separation device, and concentrating the liquid in the re-aeration tank as necessary, The liquid in the re-aeration tank is directly dehydrated without passing through the sludge separation tank and the sludge concentration storage tank.
作用 このようにすると、再曝気槽内の液を膜分離装置で濾過
処理してこの再曝気槽内の液を必要に応じて濃縮処理す
るため、これによれば従来の汚泥分離槽で処理を行った
のと同じことになる。しかも膜分離装置で濾過処理する
ことで、分離液のSS濃度が実質的にゼロになって放流水
の水質が良好になるうえに、安定した固液分離が可能に
なって、系内への原水の投入が不均等であっても問題は
生じない。Action In this way, the liquid in the re-aeration tank is filtered by the membrane separation device and the liquid in the re-aeration tank is concentrated if necessary, which allows the treatment in the conventional sludge separation tank. It will be the same as I did. Moreover, by performing filtration treatment with a membrane separation device, the SS concentration of the separated liquid becomes substantially zero, the quality of the discharged water becomes good, and stable solid-liquid separation becomes possible, and Even if the input of raw water is uneven, no problem will occur.
脱水処理に際しては、脱水機でバッチ式の処理が行われ
るが、このバッチ処理のための所定量ずつの汚泥が再曝
気槽から取り出されて直接に脱水処理される。このため
汚泥貯留槽が不要になって、脱水濾液中のアンモニア濃
度が低く安定した状態となる。また膜分離装置によって
再曝気槽から取り出す分離液の量を増減することで、脱
水に適したMLSS濃度の汚泥が再曝気槽から取り出され
る。In the dehydration treatment, a batch-type treatment is carried out by a dehydrator, and a predetermined amount of sludge for this batch treatment is taken out from the re-aeration tank and directly dehydrated. Therefore, the sludge storage tank is not needed, and the ammonia concentration in the dehydrated filtrate is low and stable. Also, by increasing or decreasing the amount of separated liquid taken out from the reaeration tank by the membrane separation device, sludge with an MLSS concentration suitable for dehydration can be taken out from the reaeration tank.
実施例 第１図において、１は硝化・脱窒素槽であり、原水２の
供給を受けるようになっている。硝化・脱窒素槽１に
は、硝酸化槽６、脱窒素槽７および再曝気槽８が、この
順序で接続されている。再曝気槽８の中には、膜分離装
置31が液内に浸漬するようにして設けられている。膜分
離装置31から取り出された分離液32は、ポンプ33によっ
て分離液貯槽34へ導かれる。Example In FIG. 1, reference numeral 1 is a nitrification / denitrification tank, which is supplied with raw water 2. A nitrification tank 6, a denitrification tank 7 and a re-aeration tank 8 are connected to the nitrification / denitrification tank 1 in this order. A membrane separator 31 is provided in the re-aeration tank 8 so as to be immersed in the liquid. The separated liquid 32 taken out from the membrane separation device 31 is introduced into a separated liquid storage tank 34 by a pump 33.
再曝気槽８からの汚泥は、その一部が循環汚泥35として
硝化・脱窒素槽１へ戻され、かつその残部が余剰汚泥36
として凝集混和槽18へ導かれている。37,38はポンプで
ある。凝集混和槽18には脱水機39が接続され、この脱水
機39としては、フィルタープレス、ベルトフィルター、
遠心脱水機など、適宜のものが利用される。脱水機39で
生じた脱水ケーキ40は系外へ排出され、脱水分離液41は
分離液貯槽34へ送られる。分離液貯槽34からの排出液42
は、図外の凝集沈殿設備へ導かれる。A part of the sludge from the re-aeration tank 8 is returned to the nitrification / denitrification tank 1 as circulation sludge 35, and the remaining part is excess sludge 36.
Is introduced into the coagulation / mixing tank 18. 37 and 38 are pumps. A dehydrator 39 is connected to the aggregating and mixing tank 18, and as the dehydrator 39, a filter press, a belt filter,
An appropriate one such as a centrifugal dehydrator is used. The dehydrated cake 40 produced in the dehydrator 39 is discharged out of the system, and the dehydrated separated liquid 41 is sent to the separated liquid storage tank 34. Discharged liquid 42 from separated liquid storage tank 34
Is led to a coagulation-sedimentation facility not shown.
再曝気槽８の中の液は、その大部分が汚泥として取り出
され、主として余剰汚泥36として脱水機39で処理され
る。このときの汚泥のMLSS濃度は5,000〜10,000mg/lが
適用である。この範囲よりも濃度が低下すると脱水に適
さなくなるため、その場合には膜分離装置31を運転し、
分離液32を取り出して再曝気槽８の中の液を濃縮するこ
とにより、MLSS濃度を調整する。濃度が適正範囲にあっ
て調整を要しない場合には、膜分離装置31を運転する必
要はない。Most of the liquid in the re-aeration tank 8 is taken out as sludge, and is mainly treated as excess sludge 36 in the dehydrator 39. The MLSS concentration of sludge at this time is 5,000 to 10,000 mg / l. When the concentration is lower than this range, it becomes unsuitable for dehydration, in that case, the membrane separation device 31 is operated,
The MLSS concentration is adjusted by taking out the separated liquid 32 and concentrating the liquid in the re-aeration tank 8. When the concentration is within the proper range and adjustment is not required, it is not necessary to operate the membrane separation device 31.
このように再曝気槽８の中に膜分離装置31を設けること
で被処理液の固液分離を行っているため、従来のような
汚泥分離槽は必要でなくなる。また膜分離装置31から取
り出される分離液32はSS濃度が実質的にゼロになるた
め、従来の汚泥分離槽で分離液を得る場合のようなSSの
流出がなくなる。よって、その後の凝集沈殿処理時の状
態が安定し、水質が良好になる。Since the membrane separation device 31 is provided in the re-aeration tank 8 in this way to perform solid-liquid separation of the liquid to be treated, a sludge separation tank as in the past is not necessary. Further, since the SS concentration of the separation liquid 32 taken out from the membrane separation device 31 becomes substantially zero, SS does not flow out as in the case of obtaining the separation liquid in the conventional sludge separation tank. Therefore, the state at the time of the subsequent coagulation-sedimentation treatment becomes stable and the water quality becomes good.
また再曝気槽８からの汚泥を直接脱水して、従来の汚泥
貯留槽をなくすようにしたため、脱水濾液中のアンモニ
ア濃度が上昇することがなく、これを低く安定した状態
に維持することができる。したがって、この点からも放
流水の水質を安定に良好状態に保つことができる。汚泥
貯留槽がなくなるので、臭気対策にもなる。Further, since the sludge from the re-aeration tank 8 is directly dehydrated so as to eliminate the conventional sludge storage tank, the ammonia concentration in the dehydrated filtrate does not increase and can be maintained in a low and stable state. . Therefore, also from this point, the quality of the discharged water can be stably maintained in a good state. Since there is no sludge storage tank, it also helps prevent odors.
このように本発明の方法は、無希釈の高負荷処理である
ため、従来の施設に若干の改造を行うだけで容易に実施
できる。たとえば上述の例では、浸漬型の膜分離装置31
を再曝気槽８の中へ入れるだけでよく、それ以外に若干
の配管切り廻しを行うだけですむ。なお膜分離装置は浸
漬型、管状内圧型など適宜のものを利用でき、必要量の
分離液32を取り出すだけのものであるため小型のもので
すむ。加えて浸漬型のものを用いれば、動力費は飛躍的
に小さくなる。また膜分離装置31を用いたことから、原
水を均等投入しなくても、安定した固液分離が可能にな
る。As described above, since the method of the present invention is a high-dilution treatment without dilution, it can be easily carried out by slightly modifying a conventional facility. For example, in the above example, the immersion type membrane separation device 31
Need only be put into the re-aeration tank 8 and in addition to that, some piping cutting is required. A suitable membrane separation device such as an immersion type or a tubular internal pressure type can be used, and only a small amount of the separation liquid 32 is taken out, so a small size is required. In addition, if the immersion type is used, the power cost will be dramatically reduced. Further, since the membrane separation device 31 is used, stable solid-liquid separation can be performed without evenly feeding raw water.
発明の効果 以上述べたように本発明によると、従来の汚泥分離槽を
なくして、再曝気槽内の液を膜分離装置により濾過する
ようにしたため、分離液のSS濃度を著しく低減すること
ができる。また、従来の汚泥貯留槽をなくして、再曝気
槽からの汚泥を直接脱水するようにしたため、脱水濾液
中のアンモニア濃度を低減することができる。よって以
上より、施設からの放流水の水質を良好なものとするこ
とができる。また汚泥貯留槽がないため臭気対策にもな
る。As described above, according to the present invention, the conventional sludge separation tank is eliminated and the liquid in the re-aeration tank is filtered by the membrane separation device, so that the SS concentration of the separated liquid can be significantly reduced. it can. Further, since the conventional sludge storage tank is eliminated and the sludge from the reaeration tank is directly dehydrated, the ammonia concentration in the dehydrated filtrate can be reduced. Therefore, from the above, the quality of the water discharged from the facility can be improved. In addition, since there is no sludge storage tank, it also helps prevent odors.
第１図は本発明の一実施例の廃水処理方法にかかる廃水
処理装置の概略構成図、第２図は従来の廃水処理方法に
かかる廃水処理装置の概略構成図である。 ８……再曝気槽、31……膜分離装置、32……分離液、36
……余剰汚泥、39……脱水機、41……脱水分離液。FIG. 1 is a schematic configuration diagram of a wastewater treatment device according to a wastewater treatment method of one embodiment of the present invention, and FIG. 2 is a schematic configuration diagram of a wastewater treatment device according to a conventional wastewater treatment method. 8: Re-aeration tank, 31: Membrane separation device, 32: Separation liquid, 36
...... Excess sludge, 39 …… dehydrator, 41 …… dehydrated separation liquid.
Claims (1)
理可能として、この再曝気槽内の液を必要に応じて濃縮
処理するとともに、この再曝気槽内の液を、汚泥分離槽
および汚泥濃縮貯留槽を通すことなしに直接に脱水処理
することを特徴とする廃水処理方法。A liquid in the re-aeration tank can be filtered by a membrane separation device, the liquid in the re-aeration tank is concentrated as necessary, and the liquid in the re-aeration tank is treated as a sludge separation tank. And a wastewater treatment method characterized by directly performing dehydration without passing through a sludge thickening storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1212191A JPH0724834B2 (en) | 1989-08-18 | 1989-08-18 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1212191A JPH0724834B2 (en) | 1989-08-18 | 1989-08-18 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0377699A JPH0377699A (en) | 1991-04-03 |
| JPH0724834B2 true JPH0724834B2 (en) | 1995-03-22 |
Family
ID=16618433
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1212191A Expired - Fee Related JPH0724834B2 (en) | 1989-08-18 | 1989-08-18 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0724834B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5433868A (en) * | 1993-09-09 | 1995-07-18 | Battelle Memorial Institute | Sewage treatment method |
| US8114293B2 (en) | 2003-10-29 | 2012-02-14 | Zenon Technology Partnership | Method of operating a water treatment plant with immersed membranes |
| US7879229B2 (en) | 2003-10-29 | 2011-02-01 | Zenon Technology Partnership | Water treatment plant with immersed membranes |
| JP4667531B2 (en) * | 2009-07-28 | 2011-04-13 | 株式会社神鋼環境ソリューション | Membrane separation activated sludge treatment apparatus and membrane separation activated sludge treatment method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62155991A (en) * | 1985-12-27 | 1987-07-10 | Hitachi Plant Eng & Constr Co Ltd | Waste water treatment device |
-
1989
- 1989-08-18 JP JP1212191A patent/JPH0724834B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0377699A (en) | 1991-04-03 |
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