JPH10309594A - Waste water treating device - Google Patents
Waste water treating deviceInfo
- Publication number
- JPH10309594A JPH10309594A JP11812297A JP11812297A JPH10309594A JP H10309594 A JPH10309594 A JP H10309594A JP 11812297 A JP11812297 A JP 11812297A JP 11812297 A JP11812297 A JP 11812297A JP H10309594 A JPH10309594 A JP H10309594A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- tank
- separation
- liquid
- biological 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.)
- Granted
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、排水を生物処理す
る生物処理手段と、この生物処理液を膜分離する膜分離
手段とを有した排水処理装置に関する。The present invention relates to a wastewater treatment apparatus having biological treatment means for biologically treating wastewater and membrane separation means for membrane-separating the biological treatment liquid.
【０００２】[0002]
【従来の技術】窒素及びリンを含む有機性排水の処理装
置として、生物処理手段と膜分離手段とを備えたものが
ある。2. Description of the Related Art As an apparatus for treating organic wastewater containing nitrogen and phosphorus, there is an apparatus provided with biological treatment means and membrane separation means.
【０００３】図２はこの排水処理装置の従来例を示す系
統図である。この排水処理装置の生物処理槽において
は、硝化処理水循環管２４によって硝化処理水を循環返
送し、凝集処理液返送管２５によって凝集処理液を返送
する。原水供給管２２より窒素やリンを含む原水を嫌気
槽１７に供給すると、原水は槽内において、脱窒菌を主
とする微生物からなる活性汚泥、硝化処理水、および凝
集処理液と、撹拌装置２３により撹拌混合される。この
混合液中に含まれる硝酸性窒素や亜硝酸性窒素が嫌気条
件下に脱窒菌の硝酸呼吸によって窒素ガスまで還元され
るとともに生物分解性有機物が分解され、槽内で脱窒さ
れた脱窒処理水が好気槽１８に流出する。FIG. 2 is a system diagram showing a conventional example of this wastewater treatment apparatus. In the biological treatment tank of this wastewater treatment apparatus, the nitrification treatment water is circulated and returned by the nitrification treatment water circulation pipe 24, and the coagulation treatment liquid is returned by the coagulation treatment liquid return pipe 25. When raw water containing nitrogen and phosphorus is supplied from the raw water supply pipe 22 to the anaerobic tank 17, the raw water is supplied into the tank with activated sludge composed of microorganisms mainly including denitrifying bacteria, nitrification-treated water, and coagulation treatment liquid, and a stirring device 23. With stirring. The nitrate nitrogen and nitrite nitrogen contained in this mixture are reduced to nitrogen gas by nitric acid respiration of the denitrifying bacteria under anaerobic conditions, and the biodegradable organic matter is decomposed. The treated water flows out to the aerobic tank 18.
【０００４】好気槽１８に流入した脱窒処理水は、ブロ
ワー３１より散気装置３２を通じて空気が供給される好
気的条件下で、槽内の硝化菌を主体とする微生物からな
る活性汚泥と混合され、この混合液中に含まれる有機性
窒素やアンモニア性窒素は硝化菌の酸化作用によって亜
硝酸性窒素や硝酸性窒素に硝化される。槽内で硝化され
た硝化処理水は、循環ポンプ２６により硝化処理水返送
管２４を通って嫌気槽１７へ返送され、再び脱窒作用を
受ける。好気槽１８内に滞留してくる余剰汚泥は汚泥引
抜管２７によって引き抜く。[0004] The denitrification-treated water flowing into the aerobic tank 18 is activated sludge comprising microorganisms mainly composed of nitrifying bacteria in the tank under aerobic conditions in which air is supplied from a blower 31 through a diffuser 32. And the organic nitrogen and ammonia nitrogen contained in the mixture are nitrified into nitrite nitrogen and nitrate nitrogen by the oxidizing action of nitrifying bacteria. The nitrification-treated water that has been nitrified in the tank is returned to the anaerobic tank 17 through the nitrification-treated water return pipe 24 by the circulation pump 26, and is subjected to the denitrification action again. Excess sludge remaining in the aerobic tank 18 is drawn out by a sludge drawing pipe 27.
【０００５】吸引ポンプ２９により膜透過水取出管３０
を通じて浸漬型膜分離装置２８に吸引負圧を作用させる
と、槽内の硝化処理水は膜分離装置２８により固液分離
されて、窒素分は除去されているがリンをリン酸イオン
の形態で含む膜透過水が膜透過水取出管３０へと取り出
される。膜透過水取出管３０へ取り出された膜透過水
は、ＲＯ（逆浸透）膜保護用のカートリッジフィルター
３３を通って、打込ポンプ３４によってＲＯ膜濾過装置
１９に圧送される。ＲＯ膜を透過した脱塩水が脱塩水取
出管３５によって取り出される。一方、リン酸イオンや
その他のイオン類並びに有機物を含む濃縮液が濃縮液返
送管３６によって凝集混和槽２０へ送られる。そして、
槽２０内で凝集剤供給管３７より供給される硫酸バン
ド、ポリ塩化アルミニウム、塩化第２鉄、ポリ硫酸第２
鉄などの凝集剤と混和され、濃縮液中のリン酸イオンや
その他のイオン類や有機物が凝集される。この凝集物を
含む凝集処理液は沈降槽２１へ送られ、リンや有機物を
含む沈降凝集物が凝集物引抜管３８によって適宜引き抜
かれるとともに、上澄液は凝集処理液返送管２５によっ
て嫌気槽１７へ返送される。[0005] The suction pump 29 is used to remove the permeated water extraction pipe 30.
When suction negative pressure is applied to the immersion type membrane separation device 28 through the, the nitrification treatment water in the tank is solid-liquid separated by the membrane separation device 28 and nitrogen content is removed, but phosphorus is converted into phosphate ions. The permeated water containing is taken out to the permeated water extraction pipe 30. The membrane permeated water taken out to the membrane permeated water extraction pipe 30 passes through a cartridge filter 33 for RO (reverse osmosis) membrane protection, and is pumped to the RO membrane filtration device 19 by a driving pump 34. Demineralized water that has passed through the RO membrane is taken out by a desalinated water extraction pipe 35. On the other hand, a concentrated solution containing phosphate ions, other ions, and organic matter is sent to the coagulation mixing tank 20 by the concentrated solution return pipe 36. And
Sulfuric acid band, polyaluminum chloride, ferric chloride, polysulfuric acid sulfuric acid supplied from flocculant supply pipe 37 in tank 20
It is mixed with an aggregating agent such as iron, and phosphate ions and other ions and organic substances in the concentrated solution are aggregated. The coagulation liquid containing the aggregates is sent to the sedimentation tank 21, and the sedimentation coagulates containing phosphorus and organic substances are appropriately extracted by the coagulation extraction pipe 38. Will be returned to
【０００６】[0006]
【発明が解決しようとする課題】生物処理手段と膜分離
手段とを組み合わせた上記図２の排水処理装置において
は、次の、のような短所があった。 生物処理槽内に浸漬型分離膜を設置する場合、膜面
の汚れを防止することと、動力（吸引ポンプ消費電力）
の低減を図ることが重要である。そして、これらのため
には、浸漬型分離膜の透過水量を少なくすることが必要
となる。ところが、上記図２の排水処理装置において
は、ＲＯ膜濾過装置１９の濃縮水に凝集剤を添加した
後、固液分離（沈降分離）し、この固液分離により得ら
れた水（上澄水）をすべて生物処理装置１７、１８へ戻
すようにしているところから嫌気槽１７への返送水量が
多くなり、浸漬型膜分離装置２８の透過水量（フラック
ス）を著しく多くしなければならない。この結果、浸漬
型膜分離装置２８の透過膜の膜面に汚れ（ゲル層）が堆
積し易いと共に、ポンプ２９の消費動力も大きい。 ＲＯ膜濾過装置１９は目詰りし易く、安定運転が難
しい。The wastewater treatment apparatus of FIG. 2 combining the biological treatment means and the membrane separation means has the following disadvantages. When installing a immersion type separation membrane in a biological treatment tank, prevent contamination of the membrane surface and power (power consumption of the suction pump).
It is important to reduce this. For these purposes, it is necessary to reduce the amount of water permeated through the immersion type separation membrane. However, in the wastewater treatment apparatus shown in FIG. 2, after adding a flocculant to the concentrated water of the RO membrane filtration apparatus 19, solid-liquid separation (sedimentation separation) is performed, and water (supernatant water) obtained by the solid-liquid separation is obtained. The amount of water returned to the anaerobic tank 17 increases from the point where all of the wastewater is returned to the biological treatment devices 17 and 18, and the amount of permeated water (flux) of the immersion type membrane separation device 28 must be significantly increased. As a result, dirt (gel layer) easily accumulates on the membrane surface of the permeable membrane of the immersion membrane separator 28, and the power consumption of the pump 29 is large. The RO membrane filtration device 19 is easily clogged, and stable operation is difficult.
【０００７】本発明は、このような問題点を解決し、浸
漬型膜分離手段の膜面の汚れ（ゲル層生成）が少なく、
ポンプ動力コストが低く、安定運転が可能な排水処理装
置を提供することを目的とする。[0007] The present invention has solved the above-mentioned problems, and has reduced contamination (gel layer formation) on the membrane surface of the immersion type membrane separation means.
It is an object of the present invention to provide a wastewater treatment device that has a low pump power cost and can be operated stably.
【０００８】[0008]
【課題を解決するための手段】本発明の排水処理装置
は、生物処理手段と、該生物処理手段の生物処理液を固
液分離処理する第１の浸漬型膜分離手段と、該浸漬型膜
分離手段からの透過水に凝集剤を添加する手段と、この
凝集剤が添加された液を固液分離処理する第２の浸漬型
膜分離手段と、からなり、該第２の浸漬型膜分離手段の
透過水を処理水として取り出し、濃縮液は生物処理手段
へ返送するようにしたことを特徴とするものである。A wastewater treatment apparatus according to the present invention comprises a biological treatment means, a first immersion type membrane separation means for performing a solid-liquid separation treatment of a biological treatment liquid of the biological treatment means, and the immersion type membrane. A means for adding a flocculant to the permeated water from the separation means, and a second immersion type membrane separation means for subjecting the liquid to which the coagulant has been added to a solid-liquid separation treatment. The permeated water of the means is taken out as treated water, and the concentrated liquid is returned to the biological treatment means.
【０００９】かかる排水処理装置においては、生物処理
手段で処理された生物処理液が第１の浸漬型膜分離手段
で膜分離される。In the wastewater treatment apparatus, the biological treatment liquid treated by the biological treatment means is subjected to membrane separation by the first immersion type membrane separation means.
【００１０】この透過液に凝集剤が添加され、第２の浸
漬型膜分離手段で膜分離処理される。この透過水が処理
水として取り出される。凝集汚泥を含む液は、この第２
の浸漬型膜分離手段から生物処理手段へ返送される。第
２の浸漬型膜分離手段においては凝集剤が添加された液
を膜分離するため、透過水量を多くすることができ、該
第２の浸漬型膜分離手段から生物処理手段へ返送される
返送液量を著しく少なくすることができる。この結果、
生物処理手段内に設けられた第１の浸漬型膜分離手段の
透過水量を少なく押えることができ、その膜面への汚れ
の堆積を減少できると共に、ポンプ動力も少なくて済
む。[0010] A coagulant is added to the permeate and subjected to a membrane separation treatment by a second immersion type membrane separation means. This permeated water is taken out as treated water. The liquid containing coagulated sludge is
Is returned from the immersion type membrane separation means to the biological treatment means. In the second immersion type membrane separation means, since the liquid to which the flocculant has been added is subjected to membrane separation, the amount of permeated water can be increased, and the returned water is returned from the second immersion type membrane separation means to the biological treatment means. The liquid volume can be significantly reduced. As a result,
The amount of permeated water of the first immersion type membrane separation means provided in the biological treatment means can be reduced, and the accumulation of dirt on the membrane surface can be reduced, and the pump power can be reduced.
【００１１】なお、第２の浸漬型膜分離手段は、ＲＯ膜
濾過装置に比べ目詰りしにくく、運転が安定している。Incidentally, the second immersion type membrane separation means is less likely to be clogged than the RO membrane filtration device, and the operation is stable.
【００１２】[0012]
【発明の実施の形態】図１は実施の形態に係る排水処理
装置の系統図である。FIG. 1 is a system diagram of a wastewater treatment apparatus according to an embodiment.
【００１３】原水配管１から導入された有機性排水は、
生物処理槽２においてブロワー３からの空気が散気管２
ａによって吹き込まれることにより好気的に生物処理さ
れ、固液分離槽４に移送される。生物処理水は、この槽
４内において、第１の浸漬型膜分離手段としての分離膜
５により固液分離される。該分離膜５によって濃縮され
た液は、返送管１４によって返送汚泥として生物処理槽
２へ返送される。The organic wastewater introduced from the raw water pipe 1 is
The air from the blower 3 in the biological treatment tank 2
By being blown by a, the biological treatment is performed aerobically and transferred to the solid-liquid separation tank 4. The biologically treated water is solid-liquid separated in the tank 4 by a separation membrane 5 as first immersion type membrane separation means. The liquid concentrated by the separation membrane 5 is returned to the biological treatment tank 2 as return sludge by the return pipe 14.
【００１４】分離膜５の透過水は吸引ポンプ６を経て凝
集槽８内に導入され、撹拌機８ａで撹拌されつつ凝集剤
及び必要ならばさらに中和剤が添加手段７により添加さ
れる。これによりリンや高分子有機物などが不溶化され
る。この薬剤が添加された液は、凝集分離槽９に導入さ
れ、第２の浸漬型膜分離手段としての分離膜１０により
固液分離され、透過水は処理水として吸引ポンプ１１を
経て取り出される。凝集分離槽９で濃縮された液は、配
管１５により凝集汚泥として生物処理槽２へ返送され
る。生物処理槽２で生成した余剰汚泥は、生物処理槽２
から配管１２により、又は固液分離槽４から配管１３に
より適宜引抜かれ、脱水機１６により脱水処理される。
脱水ケーキは系外へ排出され、脱水濾液は配管１６ａに
よって生物処理槽２へ送られる。The permeated water of the separation membrane 5 is introduced into the coagulation tank 8 via the suction pump 6, and the coagulant and, if necessary, the neutralizer are added by the adding means 7 while being stirred by the stirrer 8a. This insolubilizes phosphorus and high molecular organic substances. The liquid to which the chemical has been added is introduced into the coagulation separation tank 9 and is separated into solid and liquid by the separation membrane 10 as the second immersion type membrane separation means. The permeated water is taken out through the suction pump 11 as treated water. The liquid concentrated in the coagulation / separation tank 9 is returned to the biological treatment tank 2 as coagulated sludge by the pipe 15. Surplus sludge generated in the biological treatment tank 2 is
From the solid-liquid separation tank 4 through a pipe 13 and dewatered by a dehydrator 16.
The dehydrated cake is discharged out of the system, and the dehydrated filtrate is sent to the biological treatment tank 2 via the pipe 16a.
【００１５】なお、固液分離槽４では、分離膜５の下方
に散気管５ａを配置し、凝集分離槽９においては、分離
膜１０の下方に散気管９ａを配置している。これらの散
気管５ａ，９ａにもブロワー３から空気が供給される。In the solid-liquid separation tank 4, an air diffuser 5a is arranged below the separation membrane 5, and in the coagulation separation tank 9, an air diffuser 9a is arranged below the separation membrane 10. Air is also supplied from the blower 3 to these air diffusers 5a and 9a.
【００１６】この排水処理装置においては、第１の浸漬
型膜分離手段としての分離膜５を透過した液に凝集剤が
添加され、この凝集液が凝集分離槽９内において第２の
浸漬型膜分離手段たる分離膜１０によって固液分離され
る。この分離膜１０は、従って（未凝集状態の液を透過
処理する場合に比べ）膜面へのケーキ層堆積が少なく、
低動力にて多くの透過水を得ることができる。この結
果、配管１５から生物処理槽２へ返送される濃縮液量が
少ないものとなり、第１の浸漬型膜分離手段たる分離膜
５の透過水量を少なく押えることができ、該分離膜５の
膜面閉塞を抑制できる。加えて、吸引ポンプ６の消費動
力も少なくて済む。In this wastewater treatment apparatus, a coagulant is added to the liquid that has passed through the separation membrane 5 as the first immersion type membrane separation means, and the coagulation liquid is added to the second immersion type membrane in the coagulation separation tank 9. Solid-liquid separation is performed by the separation membrane 10 serving as separation means. Thus, the separation membrane 10 has less cake layer deposition on the membrane surface (compared to the case where the liquid in an unagglomerated state is permeated),
Many permeated water can be obtained with low power. As a result, the amount of the concentrated liquid returned from the pipe 15 to the biological treatment tank 2 is small, and the amount of permeated water of the separation membrane 5 as the first immersion type membrane separation means can be suppressed to a small amount. Surface blockage can be suppressed. In addition, the power consumption of the suction pump 6 can be reduced.
【００１７】なお、この図１の排水処理装置のその他の
作用について次に説明する。The other operation of the wastewater treatment apparatus shown in FIG. 1 will be described below.
【００１８】 生物処理槽２内での汚泥のＳＲＴ（汚
泥滞留時間）は、短いもので１０日程度以上、し尿処理
のように硝化脱窒処理する場合には１ケ月以上のものも
あり、汚泥の濃度等の性状は比較的安定している。これ
に対して配管１５から引き抜かれる凝集汚泥の場合のＳ
ＲＴは、数日以下が一般的であり、引き抜かれる汚泥の
性状は変動し易い。また、凝集槽８では、分離膜５の透
過水に凝集剤を添加しているため、槽８，９における凝
集汚泥の生成量も通常の生物処理での余剰汚泥に比較し
てはるかに少ない。これらのことから、凝集汚泥を生物
処理槽２に流入させ、余剰汚泥として引き抜くことによ
り、均質な脱水原泥が得られるという効果が奏される。
凝集槽８に添加する凝集剤としては、塩化第２鉄やポリ
硫酸鉄などの鉄塩や硫酸バンド、ＰＡＣなどのアルミニ
ウム塩が用いられる。これらにより生成した凝集汚泥は
生物処理の機能に何ら障害を与えず、むしろ、生物処理
で活性汚泥が腐敗した場合に発生するＨ2 ＳをＦｅＳや
Ｆｅ2 Ｓ3 として不溶化し、その毒性を解消することが
できる。The sludge retention time (SRT) of the sludge in the biological treatment tank 2 may be as short as about 10 days or more, and may be as long as one month or more in the case of nitrification and denitrification treatment such as night soil treatment. The properties such as concentration are relatively stable. On the other hand, in the case of coagulated sludge pulled out from the pipe 15, S
RT is generally several days or less, and the properties of sludge to be drawn are liable to fluctuate. Further, in the flocculation tank 8, since the flocculant is added to the permeated water of the separation membrane 5, the generation amount of the flocculated sludge in the tanks 8 and 9 is much smaller than the excess sludge in the ordinary biological treatment. From these facts, it is possible to obtain an effect of obtaining uniform dewatered raw sludge by flowing the coagulated sludge into the biological treatment tank 2 and extracting it as surplus sludge.
As a coagulant to be added to the coagulation tank 8, an iron salt such as ferric chloride or polyiron sulfate, a sulfate band, or an aluminum salt such as PAC is used. The coagulated sludge generated by these does not impair the function of biological treatment at all, but rather insolubilizes H 2 S generated when activated sludge rots in biological treatment as FeS or Fe 2 S 3 , eliminating its toxicity. can do.
【００１９】 ところで、一般に浸漬吸引型の分離膜
においては、その分離膜モジュールの下部より散気し、
それによる液流速により膜面でのケーキ層やゲル層の付
着を防止している。しかし、散気による液流速は通常、
膜面流速０．５〜１．０ｍ／ｓ程度と小さい値である。
（ちなみに、ＵＦ膜分離では、１．５〜２．５ｍ／ｓで
ある。）そして、前記のような曝気による液流速下で
は、ＳＳ濃度が高くなると膜面でのケーキ層、ゲル層の
形成が激しくなり、安定した膜分離性能が得られなくな
る。この傾向は凝集処理の場合、一層顕著に現われる。
本発明では凝集汚泥を生物処理槽に流入させることによ
り固液分離槽４の汚泥濃度管理が行えるようになるので
安定した分離膜性能を得やすくなる。なお、凝集汚泥を
生物処理槽２へ投入することで生物処理槽２、固液分離
槽４での汚泥濃度が多少増加する。しかし、前述のよう
に凝集汚泥の生成量は、生物処理槽２の容量および余剰
汚泥量に比較して少ないので、これによる生物処理槽
２、固液分離槽４での汚泥濃度の増加は少ない。更に、
凝集汚泥の粘性は、生物処理での活性汚泥ほど高くない
ため、これを添加しても曝気による液流に与える影響は
少ない。By the way, generally, in a immersion suction type separation membrane, air is diffused from a lower portion of the separation membrane module,
The liquid flow velocity thereby prevents the adhesion of the cake layer and the gel layer on the film surface. However, the liquid flow rate due to aeration is usually
The membrane surface flow velocity is a small value of about 0.5 to 1.0 m / s.
(By the way, in the case of UF membrane separation, the flow rate is 1.5 to 2.5 m / s.) Under the liquid flow rate caused by the aeration as described above, when the SS concentration becomes high, a cake layer and a gel layer are formed on the membrane surface. Becomes severe, and stable membrane separation performance cannot be obtained. This tendency is more pronounced in the case of coagulation treatment.
In the present invention, since the sludge concentration in the solid-liquid separation tank 4 can be controlled by flowing the coagulated sludge into the biological treatment tank, stable separation membrane performance can be easily obtained. In addition, the sludge density | concentration in the biological treatment tank 2 and the solid-liquid separation tank 4 increases a little by putting coagulated sludge into the biological treatment tank 2. However, as described above, the amount of coagulated sludge generated is smaller than the capacity of the biological treatment tank 2 and the amount of excess sludge, and therefore, the increase in the sludge concentration in the biological treatment tank 2 and the solid-liquid separation tank 4 is small. . Furthermore,
Since the viscosity of the coagulated sludge is not as high as activated sludge in biological treatment, addition of this has little effect on the liquid flow due to aeration.
【００２０】 一般に、生物処理水中には、有機物等
が生分解される際に発生する重炭酸イオン（ＨＣＯ3 -）
が含まれる。特に脱窒処理を行った場合には、除去ＮＯ
ｘ−Ｎ１ｋｇ当りＣａＣＯ3 として約７ｋｇも生成す
る。これが、凝集工程に流入するとこのＨＣＯ3 -と凝集
剤が中和反応し、凝集剤が水酸化物となり、除去すべき
リンや高分子有機物が十分には除去されず余分な凝集剤
が必要となる。従来技術では、凝集汚泥は、そのまま脱
水処理されてしまうが、本発明においては、凝集汚泥を
生物処理槽２へ流入させることにより、水酸化物となっ
た凝集剤を有効利用することができる。生物処理槽２
は、前述のように一般に長いＳＲＴで運転されるため、
流入した凝集汚泥中の未利用の水酸化物凝集剤は排水中
のリンや難生分解性高分子有機物と化合し、これらを不
溶化させる。これにより、生物処理水中のリン等の濃度
が低下し、従来のものに比較して、良好な処理水質が得
られる。In general, bicarbonate ions (HCO 3 − ) generated when biological substances are biodegraded in biologically treated water
Is included. Especially when the denitrification treatment is performed, the removal NO
About 7 kg of CaCO 3 is produced per kg of x-N. When this flows into the flocculation step, the HCO 3 - and the flocculant undergo a neutralization reaction, the flocculant becomes a hydroxide, and phosphorus and high molecular organic substances to be removed are not sufficiently removed, and an extra flocculant is required. Become. In the prior art, the coagulated sludge is directly dewatered, but in the present invention, the coagulant that has become hydroxide can be effectively used by flowing the coagulated sludge into the biological treatment tank 2. Biological treatment tank 2
Is typically driven on a long SRT as described above,
The unused hydroxide flocculant in the flocculated sludge that has flowed in combines with the phosphorus and the hardly biodegradable high molecular organic matter in the wastewater to insolubilize them. As a result, the concentration of phosphorus and the like in the biologically treated water is reduced, and a better treated water quality is obtained as compared with the conventional one.
【００２１】[0021]
【発明の効果】以上の通り、本発明の排水処理装置は、
浸漬型膜分離手段の膜面の汚れが少なくて、長期にわた
って安定運転可能である。また、膜分離処理のためのポ
ンプの消費動力が少なく、処理動力コストも低廉とな
る。As described above, the wastewater treatment apparatus of the present invention
The membrane surface of the immersion type membrane separation means is less contaminated and can be operated stably for a long time. Further, the power consumption of the pump for the membrane separation processing is small, and the processing power cost is low.
【図１】実施の形態に係る排水処理装置の系統図であ
る。FIG. 1 is a system diagram of a wastewater treatment device according to an embodiment.
【図２】従来例に係る排水処理装置の系統図である。FIG. 2 is a system diagram of a wastewater treatment device according to a conventional example.
２ 生物処理槽 ４ 固液分離槽 ５ 分離膜 ８ 凝集槽 ９ 凝集分離槽 １０ 分離膜 １６ 脱水機 2 biological treatment tank 4 solid-liquid separation tank 5 separation membrane 8 coagulation tank 9 coagulation separation tank 10 separation membrane 16 dehydrator
フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ０２Ｆ 9/00 ５０２ Ｃ０２Ｆ 9/00 ５０２Ｐ Continued on the front page (51) Int.Cl. 6 Identification code FI C02F 9/00 502 C02F 9/00 502P
Claims (1)
処理液を固液分離処理する第１の浸漬型膜分離手段と、
該浸漬型膜分離手段からの透過水に凝集剤を添加する手
段と、この凝集剤が添加された液を固液分離処理する第
２の浸漬型膜分離手段と、からなり、該第２の浸漬型膜
分離手段の透過水は処理水として取り出し、濃縮液は生
物処理手段へ返送するようにしたことを特徴とする排水
処理装置。1. Biological treatment means, first immersion type membrane separation means for performing a solid-liquid separation treatment on the biological treatment liquid of the biological treatment means,
A means for adding a flocculant to the permeated water from the immersion type membrane separation means, and a second immersion type membrane separation means for subjecting the liquid to which the coagulant has been added to a solid-liquid separation treatment, A wastewater treatment apparatus, wherein permeated water of the immersion type membrane separation means is taken out as treated water, and the concentrated liquid is returned to the biological treatment means.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11812297A JP3870481B2 (en) | 1997-05-08 | 1997-05-08 | Wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11812297A JP3870481B2 (en) | 1997-05-08 | 1997-05-08 | Wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH10309594A true JPH10309594A (en) | 1998-11-24 |
| JP3870481B2 JP3870481B2 (en) | 2007-01-17 |
Family
ID=14728590
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11812297A Expired - Fee Related JP3870481B2 (en) | 1997-05-08 | 1997-05-08 | Wastewater treatment equipment |
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| Country | Link |
|---|---|
| JP (1) | JP3870481B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011088151A (en) * | 2011-02-09 | 2011-05-06 | Toray Ind Inc | Apparatus and method for preparing regenerated water |
-
1997
- 1997-05-08 JP JP11812297A patent/JP3870481B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011088151A (en) * | 2011-02-09 | 2011-05-06 | Toray Ind Inc | Apparatus and method for preparing regenerated water |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3870481B2 (en) | 2007-01-17 |
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