JPH05104090A - Method for treating sewage or sludge and apparatus therefor - Google Patents
Method for treating sewage or sludge and apparatus thereforInfo
- Publication number
- JPH05104090A JPH05104090A JP29667991A JP29667991A JPH05104090A JP H05104090 A JPH05104090 A JP H05104090A JP 29667991 A JP29667991 A JP 29667991A JP 29667991 A JP29667991 A JP 29667991A JP H05104090 A JPH05104090 A JP H05104090A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- water
- sludge
- phosphorus
- aerobic tank
- 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
- 239000010802 sludge Substances 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000010865 sewage Substances 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 97
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 71
- 239000011574 phosphorus Substances 0.000 claims abstract description 70
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000012528 membrane Substances 0.000 claims abstract description 57
- 238000000926 separation method Methods 0.000 claims abstract description 55
- 239000000126 substance Substances 0.000 claims description 17
- 238000002425 crystallisation Methods 0.000 abstract description 4
- 230000008025 crystallization Effects 0.000 abstract description 4
- 238000005189 flocculation Methods 0.000 abstract description 2
- 230000016615 flocculation Effects 0.000 abstract description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 abstract 1
- 238000004062 sedimentation Methods 0.000 description 18
- 239000007788 liquid Substances 0.000 description 13
- 238000005345 coagulation Methods 0.000 description 12
- 230000015271 coagulation Effects 0.000 description 12
- 244000005700 microbiome Species 0.000 description 9
- 239000012510 hollow fiber Substances 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 7
- 238000000108 ultra-filtration Methods 0.000 description 5
- 241000894006 Bacteria Species 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000006228 supernatant Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000001112 coagulating effect Effects 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229920002492 poly(sulfone) Polymers 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 239000001888 Peptone Substances 0.000 description 1
- 108010080698 Peptones Proteins 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 229910052586 apatite Inorganic materials 0.000 description 1
- 210000001601 blood-air barrier Anatomy 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- VSIIXMUUUJUKCM-UHFFFAOYSA-D pentacalcium;fluoride;triphosphate Chemical compound [F-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O VSIIXMUUUJUKCM-UHFFFAOYSA-D 0.000 description 1
- 235000019319 peptone Nutrition 0.000 description 1
- 229910052585 phosphate mineral Inorganic materials 0.000 description 1
- -1 phosphorus compound Chemical class 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- VLOPEOIIELCUML-UHFFFAOYSA-L vanadium(2+);sulfate Chemical compound [V+2].[O-]S([O-])(=O)=O VLOPEOIIELCUML-UHFFFAOYSA-L 0.000 description 1
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
- Activated Sludge Processes (AREA)
- Removal Of Specific Substances (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、下水、し尿、産業廃水
等の汚水あるいは汚水処理により発生する汚泥の処理方
法およびそれを適用した汚水あるいは汚泥の処理装置に
関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating sewage such as sewage, night soil, industrial wastewater, etc. or a sludge generated by treatment of sewage, and a sewage or sludge treatment apparatus to which the method is applied.
【０００２】[0002]
【従来の技術】生物学的脱リン法は、微生物が好気状態
でリンを取り込む前に一度嫌気状態にしてリンを放出さ
せると、リンの取り込み量が著しく増加する現象を応用
したものである。生物学的リン除去方法としては、フォ
ストリップ法と嫌気−好気活性汚泥法がある。2. Description of the Related Art The biological dephosphorization method is an application of a phenomenon in which the amount of phosphorus uptake remarkably increases when microorganisms are put into an anaerobic state once to release phosphorus in the aerobic state. .. Biological phosphorus removal methods include the fosstrip method and the anaerobic-aerobic activated sludge method.
【０００３】フォストリップ法は、例えば、図３に示し
たフローが挙げられ、基本的には、流入原水２０を導入
して生物学的に処理する好気槽２１、好気槽２１からの
活性汚泥スラリーを含む処理液を沈殿処理し、上澄水を
処理水３０とする沈殿池２２、該沈殿池２２において濃
縮され、かつリンを過剰摂取した汚泥が導入されるリン
ストリッパー２３、リンストリッパー２３において内生
呼吸状態、即ち嫌気状態でリンを放出させ、リン濃度の
高い上澄水と石灰等の化学薬品２４を添加して効率的に
凝集沈殿させるための凝集沈殿池２５から概略構成され
ている。そして、沈殿池２２で余剰となった汚泥は、余
剰汚泥２６として排出される。リンストリッパー２３で
処理された汚泥は、返送汚泥２７として、好気槽２１に
返送され、凝集沈殿池２５で化学沈殿処理された凝集汚
泥２８は、排出され、脱リンされた凝沈処理水２９は、
処理水３０として放流あるいはその一部を流入原水２０
に混合し、再処理にまわされる。The fostrip method includes, for example, the flow shown in FIG. 3. Basically, the aerobic tank 21 for introducing the inflowing raw water 20 and biologically treating it, and the activity from the aerobic tank 21. In the settling tank 22 in which the treatment liquid containing the sludge slurry is subjected to a precipitation treatment, and the supernatant water is the treated water 30, and in the rinse stripper 23 and the rinse stripper 23 into which the sludge concentrated in the sedimentation tank 22 and into which phosphorus is excessively ingested are introduced. It is generally configured by a flocculation sedimentation tank 25 for releasing phosphorus in an endogenous respiration state, that is, in an anaerobic state, and adding a chemical agent 24 such as supernatant water having a high phosphorus concentration and lime to efficiently coagulate and precipitate. The excess sludge in the settling tank 22 is discharged as excess sludge 26. The sludge treated by the rinsing stripper 23 is returned to the aerobic tank 21 as the return sludge 27, and the coagulated sludge 28 that has been chemically precipitated in the coagulation sedimentation tank 25 is discharged and dephosphorized. Is
Discharge as treated water 30 or part of it as inflow raw water 20
It is then mixed and reprocessed.
【０００４】この方法は、脱リン槽２３に維持できる汚
泥量は沈殿池２２の重力沈殿に依存しているため汚泥か
らのリン放出量に変動が生じ不安定となる場合があっ
た。また、脱リン槽の上澄水は固液分離が不完全なため
ＳＳを若干含んでおりリン凝集に必要な量以上の薬品が
消費されるため不経済である。また、嫌気−好気活性汚
泥法は、図４に示したフローが挙げられ、流入原水２０
を好気槽２１の前段に設けた嫌気槽３１に導入し、嫌気
槽３１で汚泥より放出されたリンを好気槽２１にて汚泥
に取り込み、沈殿池２２にて上澄水を処理水３０とする
一方、沈殿汚泥をリン含有率の高い余剰汚泥３２として
その大部を系外に排出し、一部を返送汚泥３３として嫌
気槽３１に返送する方法である。In this method, the amount of sludge that can be maintained in the dephosphorization tank 23 depends on the gravity settling in the settling tank 22, so that the amount of phosphorus released from the sludge may fluctuate and become unstable. In addition, the supernatant water of the dephosphorization tank contains a small amount of SS due to incomplete solid-liquid separation, and it is uneconomical because more chemicals than necessary for phosphorus aggregation are consumed. The anaerobic-aerobic activated sludge method includes the flow shown in FIG.
Is introduced into the anaerobic tank 31 provided before the aerobic tank 21, phosphorus released from the sludge in the anaerobic tank 31 is taken into the sludge in the aerobic tank 21, and the supernatant water is treated with the treated water 30 in the settling tank 22. On the other hand, the settled sludge is discharged as a surplus sludge 32 having a high phosphorus content, the majority of which is discharged to the outside of the system, and a part of the sludge is returned to the anaerobic tank 31 as return sludge 33.
【０００５】この方法において、 （１）Ｐ／ＢＯＤ比が高い場合 （２）原水溶解性ＢＯＤ濃度が低い場合 等は、汚泥中のリン含有率に限界があるため、リンの除
去率が低下する。この改善策として特公昭５８−３９５
９９号公報に示されているように嫌気槽と好気槽との間
に中間沈殿池を設け、分離水中のリンを化学的に固定化
し、生物学的に除去できないリンを除去する方法があ
る。この方法は固液分離に沈殿池を用いているため、汚
水性状に左右され、運転管理が複雑であると言う問題、
沈殿池の分離面積を大きくとらざるを得ないと言う問題
があった。In this method, (1) when the P / BOD ratio is high (2) when the raw water-soluble BOD concentration is low, etc., there is a limit to the phosphorus content in the sludge, so the phosphorus removal rate decreases. .. As a measure for this improvement, Japanese Patent Publication No. 58-395
As disclosed in Japanese Patent Publication No. 99, there is a method of providing an intermediate settling tank between an anaerobic tank and an aerobic tank to chemically fix phosphorus in the separated water to remove phosphorus that cannot be biologically removed. .. Since this method uses a settling tank for solid-liquid separation, it depends on the state of wastewater and the problem that operation management is complicated,
There was a problem that the separation area of the sedimentation tank had to be large.
【０００６】[0006]
【発明が解決しようとする課題】本発明は、上記の従来
技術における問題点を解消するため、生物学的脱リン法
と膜分離技術を組合せることで安定したリン除去を可能
とした汚水あるいは汚泥処理方法およびそれを適用した
汚水あるいは汚泥処理装置を提供することを目的とす
る。DISCLOSURE OF THE INVENTION In order to solve the above-mentioned problems in the prior art, the present invention uses a biological dephosphorization method and a membrane separation technique in combination to enable stable phosphorus removal or wastewater. An object of the present invention is to provide a sludge treatment method and a wastewater or a sludge treatment device to which the sludge treatment method is applied.
【０００７】[0007]
【課題を解決するための手段】上記目的は、 嫌気槽を好気槽の後段に設けると共に好気槽及び嫌
気槽内に分離膜を設け、汚泥と水とを分離し、好気槽で
分離された水は処理水として導出し、嫌気槽内で分離さ
れた水はリンを化学的処理によって除去することを特徴
とする汚水あるいは汚泥処理方法、 嫌気槽を好気槽の後段に設けると共に好気槽に処理
水を導出するための分離膜を浸漬配備し、嫌気槽にリン
含有分離水を得るための分離膜を浸漬配備し、及び前記
リン含有分離水のリンを除去するための化学処理装置を
配備したことを特徴とする汚水あるいは汚泥処理装置、 嫌気槽を好気槽の前段に設けると共に好気槽及び嫌
気槽内に分離膜を設け、汚泥と水とを分離し、好気槽で
分離された水は処理水として導出し、嫌気槽内で分離さ
れた水はリンを化学的処理によって除去することを特徴
とする汚水あるいは汚泥処理方法、および 嫌気槽を好気槽の前段に設けると共に好気槽に処理
水を導出するための分離膜を浸漬配備し、嫌気槽にリン
含有分離水を得るための分離膜を浸漬配備し、前記リン
含有分離水のリンを除去するための化学処理装置を配備
したことを特徴とする汚水あるいは汚泥処理装置、によ
り達成できる。[Means for Solving the Problems] The above-mentioned object is to install an anaerobic tank in the latter stage of the aerobic tank and to provide a separation membrane in the aerobic tank and the anaerobic tank to separate sludge and water and separate them in the aerobic tank. The treated water is discharged as treated water, and the water separated in the anaerobic tank removes phosphorus by a chemical treatment. A method for treating sewage or sludge, in which an anaerobic tank is provided after the aerobic tank. A separation membrane for deriving the treated water is immersed in the air tank, a separation membrane for obtaining the phosphorus-containing separation water is immersed in the anaerobic tank, and a chemical treatment for removing the phosphorus in the phosphorus-containing separation water. A sewage or sludge treatment device characterized by the provision of a device, an anaerobic tank was installed in front of the aerobic tank, and a separation membrane was installed in the aerobic tank and the anaerobic tank to separate the sludge from the water and the aerobic tank. The water separated in was discharged as treated water and separated in the anaerobic tank. Is a method for treating sewage or sludge, which is characterized by removing phosphorus by a chemical treatment, and an anaerobic tank is provided in front of the aerobic tank, and a separation membrane for deriving the treated water is immersed in the aerobic tank. A sewage or sludge treatment device characterized in that a separation membrane for obtaining phosphorus-containing separated water is immersed in an anaerobic tank and a chemical treatment device for removing phosphorus in the phosphorus-containing separated water is provided. ..
【０００８】本発明およびの原理は、リン含有汚水
を好気槽にて生物学的に処理してＢＯＤを酸化処理する
と共に溶解リンを微生物に吸収させ、好気槽内に浸漬し
て設けられる分離膜により生物学的処理水を分離しする
と共にリンを吸収した微生物を主とする活性汚泥スラリ
ーを嫌気槽へ移送し、嫌気槽内で吸収したリンを放出せ
しめ嫌気槽内に浸漬設置された分離膜により高濃度のリ
ン含有分離水を得、これを化学的処理してリン化合物と
して沈殿もしくは晶析させることによりリン、ＢＯＤ、
ＳＳ等を除去した処理水を得る構成にある。そして、嫌
気槽でリンを放出した微生物を好気槽に循環使用する。The principle of the present invention is provided by biologically treating phosphorus-containing wastewater in an aerobic tank to oxidize BOD and at the same time allow dissolved microorganisms to be absorbed by microorganisms and immersing it in the aerobic tank. The biologically treated water was separated by a separation membrane, and the activated sludge slurry mainly containing microorganisms that absorbed phosphorus was transferred to the anaerobic tank, and the absorbed phosphorus was released in the anaerobic tank, and it was immersed in the anaerobic tank. Separation water containing a high concentration of phosphorus is obtained from the separation membrane, and the treated water is chemically treated to precipitate or crystallize as a phosphorus compound, whereby phosphorus, BOD,
It is configured to obtain treated water from which SS and the like have been removed. Then, the microorganisms that released phosphorus in the anaerobic tank are circulated and used in the aerobic tank.
【０００９】本発明およびは、上記およびにお
いて、嫌気槽の処理を好気槽の処理の前で行うものであ
り、その原理は、およびと同様であるが、ただ、嫌
気槽の分離水を化学的処理によってリンを除去すると共
に微生物を主とする活性汚泥スラリーを好気槽へ移送
し、この好気槽でＢＯＤ酸化、リンの脱リン等の生物学
的除去処理を行い、好気槽に設けられた分離膜によりリ
ン、ＢＯＤ、ＳＳ等が除去され、処理水を得る点であ
り、リンを貯留した微生物等を嫌気槽に循環させる構成
にある。In the present invention and, in the above and above, the treatment of the anaerobic tank is performed before the treatment of the aerobic tank, and the principle thereof is the same as and, except that the separated water in the anaerobic tank is chemically treated. The phosphorus is removed by mechanical treatment and the activated sludge slurry mainly containing microorganisms is transferred to the aerobic tank, and the biological removal treatment such as BOD oxidation and phosphorus dephosphorization is performed in the aerobic tank. Phosphorus, BOD, SS, and the like are removed by the provided separation membrane, and treated water is obtained, and microorganisms and the like that store phosphorus are circulated in the anaerobic tank.
【００１０】本発明において、嫌気槽、好気槽に使用さ
れる微生物は、従来法で使用された公知のものが適用で
き、少なくとも嫌気槽と好気槽間を循環できる上記リン
の吸収、排出の代謝が可能な菌（以下、脱リン菌と言
う）が含有されておればよい。本発明において適用でき
る装置構成は任意であり、本発明及びの嫌気槽、好
気槽、分離膜、リン含有分離水のリンを除去するための
化学処理装置の構造、構成も上記思想を満足すれば、特
に制限はなく従来公知の構成が採用できる。例えば、嫌
気槽は、少なくとも脱リン菌によるリンの排出機能が維
持されればよい。また、好気槽は、脱リン菌等によるＢ
ＯＤの酸化とリンの吸収が可能となるための溶存酸素を
確保できる槽構成が挙げられ、例えば、散気装置等を槽
下部に設けた構成が挙げられる。また分離膜の嫌気槽お
よび好気槽における配備方法も任意であり、被処理液に
浸漬され、膜分離水において汚泥等のＳＳが完全に排除
されるように配備、保持されておればよい。前記リンを
除去するための化学処理装置としては、凝集処理剤を使
用する凝沈法においては、凝沈槽、晶析脱リン法におい
てはリン酸塩鉱物等のリン除去材が挙げられる。In the present invention, as the microorganisms used in the anaerobic tank and the aerobic tank, known microorganisms used in the conventional method can be applied, and at least the absorption and discharge of phosphorus can be circulated between the anaerobic tank and the aerobic tank. A bacterium capable of metabolizing (hereinafter referred to as a dephosphorization bacterium) may be contained. The apparatus configuration applicable in the present invention is arbitrary, and the structure and configuration of the present invention and the anaerobic tank, aerobic tank, separation membrane, and chemical treatment apparatus for removing phosphorus containing phosphorus-containing separated water also satisfy the above idea. However, there is no particular limitation and a conventionally known configuration can be adopted. For example, in the anaerobic tank, at least the function of excreting phosphorus by dephosphorization bacteria may be maintained. In the aerobic tank, B due to dephosphorization bacteria etc.
Examples of the configuration include a tank capable of ensuring dissolved oxygen for enabling oxidation of OD and absorption of phosphorus, and for example, a configuration in which an air diffuser or the like is provided in the lower portion of the tank. Further, the method of disposing the separation membrane in the anaerobic tank and the aerobic tank is also arbitrary, and it may be arranged and held so that SS such as sludge is completely removed from the membrane separation water by being immersed in the liquid to be treated. Examples of the chemical treatment device for removing phosphorus include a coagulation tank in the coagulation method using a coagulation treatment agent, and a phosphorus removal material such as a phosphate mineral in the crystallization dephosphorization method.
【００１１】また、本発明における被処理液の処理条
件、運転条件も任意であり、適宜被処理液の性状、例え
ば、ＢＯＤ濃度、溶解リン濃度等に応じて適宜設定でき
る。運転条件としては、水温、被処理液量、凝集沈殿設
備水量（嫌気槽からの膜分離水に含まれるリンを凝沈さ
せるための設備容積）、嫌気槽あるいは好気槽からの返
送汚泥量、好気槽容量、嫌気槽容量、好気槽のＭＬＳＳ
濃度、嫌気槽のＭＬＳＳ濃度、嫌気槽及び好気槽に設け
た分離膜の表面膜面積、分離膜の孔サイズ、分離膜の差
圧、好気槽への酸素供給量等が挙げられる。The treatment conditions and operating conditions of the liquid to be treated in the present invention are also arbitrary, and can be appropriately set according to the properties of the liquid to be treated, such as the BOD concentration and the dissolved phosphorus concentration. Operating conditions include water temperature, amount of liquid to be treated, amount of coagulation-sedimentation facility water (equipment volume for coagulating phosphorus contained in membrane separation water from anaerobic tank), amount of sludge returned from anaerobic tank or aerobic tank, Aerobic tank capacity, Anaerobic tank capacity, Aerobic tank MLSS
The concentration, the MLSS concentration of the anaerobic tank, the surface membrane area of the separation membrane provided in the anaerobic tank and the aerobic tank, the pore size of the separation membrane, the differential pressure of the separation membrane, the oxygen supply amount to the aerobic tank, and the like can be mentioned.
【００１２】又、本発明においては、嫌気槽と好気槽は
各１基で十分であるが、所望により一方または両方を複
数以上組み合わせてもよい。また、分離膜からのリン含
有分離水は、前述の通り化学的処理として凝集沈殿処理
の他、晶析脱リン等の任意の処理をしてもよく、またこ
れらを併用してもよい。なお、化学的処理によってリン
を除去された処理水は好気槽へ導入するようにしてもよ
い。In the present invention, one anaerobic tank and one aerobic tank are sufficient, but one or both may be combined if desired. The phosphorus-containing separated water from the separation membrane may be subjected to any treatment such as crystallization and dephosphorization in addition to the coagulation-precipitation treatment as the chemical treatment as described above, or may be used in combination. The treated water from which phosphorus has been removed by the chemical treatment may be introduced into the aerobic tank.
【００１３】また、汚泥を対象とした場合には、汚泥の
濃縮も容易に行える。When sludge is used, sludge can be easily concentrated.
【００１４】[0014]
【作用】従来の生物脱リン法においては、汚泥の固液分
離に重力沈殿池を用いているため、嫌気槽、好気槽ＭＬ
ＳＳ濃度は、３０００ｍｇ／Ｌ（リットル）前後であっ
た。本発明のように汚泥の固液分離に分離膜を用いるこ
とで嫌気槽、好気槽のＭＬＳＳ濃度は、１０，０００〜
２０，０００ｍｇ／Ｌまで上げることが可能となり、従
来法の１／３倍〜１／６倍に装置を小型化できる。ま
た、Ｐ／ＢＯＤ比が、例えば、０．０５〜０．０８と高
い場合でも嫌気槽内で高濃度となったリンを容易に分離
水とともに回収できるため、化学的な固定を効率的に行
うことができる。尚、従来法では、Ｐ／ＢＯＤ比は０．
０４〜０．０５に制御する必要がある。In the conventional biological dephosphorization method, since the gravity sedimentation tank is used for solid-liquid separation of sludge, anaerobic tank and aerobic tank ML.
The SS concentration was around 3000 mg / L (liter). By using a separation membrane for solid-liquid separation of sludge as in the present invention, the MLSS concentration in the anaerobic tank and the aerobic tank is 10,000 to
It is possible to increase up to 20,000 mg / L, and the apparatus can be downsized to 1/3 to 1/6 times the conventional method. Further, even when the P / BOD ratio is as high as 0.05 to 0.08, for example, phosphorus having a high concentration in the anaerobic tank can be easily recovered together with the separated water, so that the chemical fixation is efficiently performed. be able to. In the conventional method, the P / BOD ratio is 0.
It is necessary to control to 04-0.05.
【００１５】嫌気槽、好気槽に用いる分離膜は精密濾過
膜あるいは限外濾過膜を中空糸膜、キャピラリー膜、チ
ューブラー膜、平膜いずれかのモジュールにしたものが
適しているが、好ましくは精密濾過膜あるいは中空糸状
のモジュールにしたものが良い。各槽に設置する膜のモ
ジュール数は各処理水の量等により調節すれば良い。嫌
気槽で分離される分離水の中のリン固定には、Ｆｅ、Ａ
ｌ、Ｃａ塩を用いた凝沈法あるいはＣａとＰとのアパタ
イトを生成させる晶析脱リン法の適用が可能である。中
間沈殿池を用いた嫌気−好気活性汚泥法の固液分離水及
びフォストリップ法においてリンストリッパーの分離水
にはＳＳが多く含まれているため、液中のリンを化学的
に固定する以上に薬品の注入が多く必要であったが、本
発明のように分離膜を用いるとＳＳ分は完全に除去でき
るため、分離水中のリン量に対応して薬品の添加を行え
ばよく、薬品のランニングコストの低減ができる。The separation membrane used in the anaerobic tank or the aerobic tank is preferably a microfiltration membrane or an ultrafiltration membrane which is a module of any of hollow fiber membrane, capillary membrane, tubular membrane and flat membrane, but it is preferable. Is preferably a microfiltration membrane or a hollow fiber module. The number of membrane modules installed in each tank may be adjusted according to the amount of each treated water. For fixing phosphorus in the separated water separated in the anaerobic tank, Fe, A
It is possible to apply a precipitation method using Ca salt or a crystallization dephosphorization method for forming apatite of Ca and P. Since the solid-liquid separation water of the anaerobic-aerobic activated sludge method using the intermediate sedimentation tank and the separation water of the phosphorus stripper in the fosstrip method contain a large amount of SS, it is necessary to chemically fix the phosphorus in the solution. Although it was necessary to inject a large amount of chemicals in the above, since the SS content can be completely removed by using the separation membrane as in the present invention, the chemicals may be added according to the amount of phosphorus in the separation water. The running cost can be reduced.
【００１６】このように本発明を生物学的脱リン法に適
用することで、従来の生物学的脱リン法を改善し、装置
がコンパクト化出来、運転管理も容易となる。なお、ア
ンモニア性窒素も除去する場合には、脱窒素槽を付設す
れば構わない。As described above, by applying the present invention to the biological dephosphorization method, the conventional biological dephosphorization method is improved, the apparatus can be made compact, and the operation management becomes easy. If ammonia nitrogen is also removed, a denitrification tank may be attached.
【００１７】[0017]
【実施例】以下、本発明を実施例により具体的に説明す
るが、本発明はこれらの実施例に限定されるものではな
い。 実施例１（嫌気槽が好気槽の後段にある場合） 図１に処理フローを示す。原水（例えば下水）１２は、
リン放出後の返送汚泥（返送汚泥ライン１３から）と共
に好気槽１に導入され、原水中のリンとＢＯＤは除去さ
れる。好気槽１はブロワー５より供給された空気によ
り、好気的状態が維持される。好気槽、嫌気槽にはそれ
ぞれ分離膜３が設置され、その分離膜３は中空糸限外濾
過膜を用いている。好気槽に設置した分離膜により汚泥
と水に分離され、好気槽分離水１６はポンプ７により導
出される。一方、活性汚泥スラリーは水中攪拌器６にて
混合される嫌気槽２に移送され、嫌気槽に設置した分離
膜により嫌気槽内で活性汚泥から放出されたリンを高濃
度に含む水がポンプ８によって分離され、分離水は凝集
沈殿設備１１に供給され、凝集沈殿においては、硫酸バ
ン土、ＮａＯＨによりリンを固定して液中より除去され
る。凝沈処理水１５は、好気槽分離水１６と混合・導出
あるいは好気槽に導かれる。また、凝集物は、排出ポン
プ１７より排出される。余剰汚泥は、例えば、排出ポン
プ１０で排出される。EXAMPLES The present invention will now be specifically described with reference to examples, but the present invention is not limited to these examples. Example 1 (when the anaerobic tank is in the latter stage of the aerobic tank) FIG. 1 shows a processing flow. Raw water (for example, sewage) 12
It is introduced into the aerobic tank 1 together with the returned sludge (from the returned sludge line 13) after phosphorus is released, and phosphorus and BOD in the raw water are removed. The aerobic tank 1 is maintained in an aerobic state by the air supplied from the blower 5. A separation membrane 3 is installed in each of the aerobic tank and the anaerobic tank, and the separation membrane 3 uses a hollow fiber ultrafiltration membrane. The separation membrane installed in the aerobic tank separates it into sludge and water, and the aerobic tank separated water 16 is drawn out by the pump 7. On the other hand, the activated sludge slurry is transferred to the anaerobic tank 2 which is mixed by the underwater agitator 6, and the water containing a high concentration of phosphorus released from the activated sludge in the anaerobic tank is pumped by the separation membrane installed in the anaerobic tank. The separated water is supplied to the coagulation-sedimentation facility 11, and in the coagulation-sedimentation, phosphorus is fixed by vanadium sulfate and NaOH to be removed from the liquid. The coagulation / sedimentation treated water 15 is mixed with and discharged from the aerobic tank separated water 16 or is introduced into the aerobic tank. Further, the aggregate is discharged from the discharge pump 17. Excess sludge is discharged by the discharge pump 10, for example.
【００１８】次に図１に示すフローにて人工廃水を用い
て行った実験結果の一例を示す。表１に示すグルコー
ス、ペプトンを主成分とした人工廃水を用いて実験を行
った。結果の一例を表２に示す。表２より明らかなよう
に、リン除去率９５％以上と良好な結果であった。ま
た、嫌気槽、好気槽に設置した分離膜の洗浄も１年間で
１回程度で運転可能であった。Next, an example of the result of an experiment conducted using artificial wastewater in the flow shown in FIG. 1 will be shown. Experiments were conducted using artificial wastewater containing glucose and peptone as main components shown in Table 1. Table 2 shows an example of the results. As is clear from Table 2, the phosphorus removal rate was 95% or more, which was a good result. Moreover, the cleaning of the separation membranes installed in the anaerobic tank and the aerobic tank could be operated about once a year.
【００１９】[0019]
【表１】 [Table 1]
【００２０】[0020]
【表２】 [Table 2]
【００２１】〔運転条件〕 水温 ２５℃ 原水水量 ２５０Ｌ／日 処理水量（好気槽分離水） ２００Ｌ／日 凝集沈殿設備水量 ５０Ｌ／日 返送汚泥量 ２５０Ｌ／日 好気槽容量 １０Ｌ 嫌気槽容量 ４Ｌ 好気槽のＭＬＳＳ濃度 １７０００ｍｇ／Ｌ 嫌気槽のＭＬＳＳ濃度 ２００００ｍｇ／Ｌ 好気槽に設置した中空糸膜（注）面積 ２．０ｍ2 嫌気槽に設置した中空糸膜（注）面積 １．０ｍ2 注：ポリスルホン製限外濾過膜 実施例２（嫌気槽が好気槽の前段にある場合） 図２に処理フローを示す。原水（例えば、下水）１２は
返送汚泥（返送汚泥ライン１３から）と共に嫌気槽２で
混合される。嫌気槽では水中攪拌器６により汚泥は混合
され、原水中のＢＯＤ成分は汚泥に摂取され、一方、リ
ンは放出される。嫌気槽、好気槽にそれぞれ設置された
分離膜３は中空糸限外濾過膜を用いている。嫌気槽に設
置した分離膜により、汚泥より放出されたリンは嫌気槽
分離水１４として系外に排出され、凝集沈殿設備１１に
供給される。凝集沈殿においては、硫酸バン土、ＮａＯ
Ｈが注入され、リンを固定化して液中より除去される。
凝沈処理水１５は好気槽１に供給あるいは好気槽分離水
１６と混合・導出される。[Operating conditions] Water temperature 25 ° C. Raw water amount 250 L / day Treated water amount (aerobic tank separated water) 200 L / day Coagulation sedimentation facility water amount 50 L / day Return sludge amount 250 L / day Aerobic tank capacity 10 L Anaerobic tank capacity 4 L Good Air tank MLSS concentration 17,000 mg / L Anaerobic tank MLSS concentration 20000 mg / L Hollow fiber membrane (Note) area 2.0 m 2 installed in aerobic tank Hollow fiber membrane (Note) area 1.0 m 2 Note installed in anaerobic tank : Polysulfone Ultrafiltration Membrane Example 2 (when anaerobic tank is in front of aerobic tank) FIG. 2 shows a processing flow. Raw water (for example, sewage) 12 is mixed with return sludge (from return sludge line 13) in anaerobic tank 2. In the anaerobic tank, the sludge is mixed by the underwater agitator 6, and the BOD component in the raw water is taken up by the sludge, while phosphorus is released. The separation membranes 3 installed in the anaerobic tank and the aerobic tank are hollow fiber ultrafiltration membranes. Due to the separation membrane installed in the anaerobic tank, phosphorus released from the sludge is discharged outside the system as anaerobic tank separated water 14 and supplied to the coagulating sedimentation facility 11. In coagulating sedimentation, van sulfate, NaO
H is injected to immobilize phosphorus and remove it from the solution.
The coagulation / sedimentation water 15 is supplied to the aerobic tank 1 or mixed / derived with the aerobic tank separated water 16.
【００２２】好気槽では残存ＢＯＤと液中に放出された
リンが汚泥に摂取される。槽内に設置した分離膜により
汚泥と水とに分離され、好気槽分離水１６は系外に導出
される。余剰汚泥は返送汚泥ライン１３より排出ポンプ
１０を用い定期的に排出される。また、凝沈物は、排出
ポンプ１７により排出される。実施例１と同様な人工廃
水を用いた実験結果を表３に示す。実施例１と同様なリ
ン除去成績を示している。In the aerobic tank, residual BOD and phosphorus released in the liquid are taken up by sludge. The separation membrane installed in the tank separates it into sludge and water, and the aerobic tank separation water 16 is led out of the system. Excess sludge is periodically discharged from the returning sludge line 13 using the discharge pump 10. Further, the sediment is discharged by the discharge pump 17. Table 3 shows the experimental results using the same artificial wastewater as in Example 1. The phosphorus removal results similar to those in Example 1 are shown.
【００２３】[0023]
【表３】 [Table 3]
【００２４】〔運転条件〕 水温 ２５℃ 原水水量 ２５０Ｌ／日 凝集沈殿設備水量 ３５Ｌ／日 返送汚泥量 ２５０Ｌ／日 処理水量（嫌気槽分離水） ２５０Ｌ／日 好気槽容量 １０Ｌ 嫌気槽容量 ７Ｌ 嫌気槽のＭＬＳＳ濃度 １００００ｍｇ／Ｌ 好気槽のＭＬＳＳ濃度 ２００００ｍｇ／Ｌ 嫌気槽に設置した中空糸膜（注）面積 ０．７ｍ2 好気槽に設置した中空糸膜（注）面積 ２．５ｍ2 注：ポリスルホン製限外濾過膜[Operating conditions] Water temperature 25 ° C. Raw water amount 250 L / day Coagulation sedimentation facility water amount 35 L / day Return sludge amount 250 L / day Treated water amount (anaerobic tank separated water) 250 L / day Aerobic tank capacity 10 L Anaerobic tank capacity 7 L Anaerobic tank MLSS concentration of 10000 mg / L MLSS concentration of aerobic tank 20000 mg / L Hollow fiber membrane (Note) area 0.7m 2 installed in anaerobic tank Hollow fiber membrane (Note) area 2.5m 2 installed in aerobic tank Note: Polysulfone ultrafiltration membrane
【００２５】[0025]
【発明の効果】以上の結果からも明らかのように本発明
のように生物脱リン法と膜分離技術を組合せることによ
り、安定した処理ができ、かつ汚泥の固液分離を膜で行
えるため、装置が簡略化され運転管理も容易となった。As is clear from the above results, by combining the biological dephosphorization method and the membrane separation technique as in the present invention, stable treatment can be performed and solid-liquid separation of sludge can be performed by the membrane. The equipment has been simplified and operation management has become easier.
【図１】本発明の内、嫌気槽を好気槽の後段に設けたフ
ローの一例を示す図である。FIG. 1 is a diagram showing an example of a flow in which an anaerobic tank is provided in a subsequent stage of an aerobic tank in the present invention.
【図２】本発明の内、嫌気槽を好気槽の前段に設けたフ
ローの一例を示す図である。FIG. 2 is a diagram showing an example of a flow of the present invention in which an anaerobic tank is provided upstream of an aerobic tank.
【図３】従来のフォストリップ法のフローを示す図であ
る。FIG. 3 is a diagram showing a flow of a conventional fosstrip method.
【図４】従来の嫌気−好気活性汚泥法のフローを示す図
である。FIG. 4 is a diagram showing a flow of a conventional anaerobic-aerobic activated sludge method.
１ 好気槽 ２ 嫌気槽 ３ 分離膜 ４ 散気板 ５ ブロワー ６ 水中攪拌器 ７ ポンプ ８ ポンプ ９ 返送汚泥ポンプ 10 排出ポンプ 11 凝集沈殿設備 12 原水 13 返送汚泥ライン 14 嫌気槽分離水 15 凝沈処理水 16 嫌気槽分離水 17 排出ポンプ 20 流入原水 21 好気槽 22 沈殿池 23 リンストリッパー 24 化学薬品 25 凝集沈殿池 26 余剰汚泥 27 返送汚泥 28 凝集汚泥 29 凝沈処理水 30 処理水 31 嫌気槽 32 余剰汚泥 33 返送汚泥 1 aerobic tank 2 anaerobic tank 3 separation membrane 4 diffuser plate 5 blower 6 submersible stirrer 7 pump 8 pump 9 return sludge pump 10 discharge pump 11 coagulation sedimentation facility 12 raw water 13 return sludge line 14 anaerobic tank separation water 15 coagulation treatment Water 16 Anaerobic tank Separation water 17 Discharge pump 20 Inflow raw water 21 Aerobic tank 22 Sedimentation tank 23 Rinse stripper 24 Chemicals 25 Coagulation sedimentation tank 26 Excess sludge 27 Return sludge 28 Coagulation sludge 29 Coagulated water 30 Treated water 31 Anaerobic tank 32 Excess sludge 33 Return sludge
Claims (4)
気槽及び嫌気槽内に分離膜を設け、汚泥と水とを分離
し、好気槽で分離された水は処理水として導出し、嫌気
槽内で分離された水はリンを化学的処理によって除去す
ることを特徴とする汚水あるいは汚泥処理方法。1. An anaerobic tank is provided downstream of the aerobic tank, and a separation membrane is provided in the aerobic tank and the anaerobic tank to separate sludge and water, and the water separated in the aerobic tank is discharged as treated water. However, the water separated in the anaerobic tank is a sewage or sludge treatment method characterized by removing phosphorus by a chemical treatment.
気槽に処理水を導出するための分離膜を浸漬配備し、嫌
気槽にリン含有分離水を得るための分離膜を浸漬配備
し、及び前記リン含有分離水のリンを除去するための化
学処理装置を配備したことを特徴とする汚水あるいは汚
泥処理装置。2. An anaerobic tank is provided in the latter stage of the aerobic tank, a separation membrane for deriving treated water is immersed in the aerobic tank, and a separation membrane for obtaining phosphorus-containing separated water is immersed in the anaerobic tank. And a chemical treatment device for removing phosphorus from the phosphorus-containing separated water, the sewage or sludge treatment device.
気槽及び嫌気槽内に分離膜を設け、汚泥と水とを分離
し、好気槽で分離された水は処理水として導出し、嫌気
槽内で分離された水はリンを化学的処理によって除去す
ることを特徴とする汚水あるいは汚泥処理方法。3. An anaerobic tank is provided in front of the aerobic tank, and a separation membrane is provided in the aerobic tank and the anaerobic tank to separate sludge and water, and the water separated in the aerobic tank is discharged as treated water. However, the water separated in the anaerobic tank is a sewage or sludge treatment method characterized by removing phosphorus by a chemical treatment.
気槽に処理水を導出するための分離膜を浸漬配備し、嫌
気槽にリン含有分離水を得るための分離膜を浸漬配備
し、前記リン含有分離水のリンを除去するための化学処
理装置を配備したことを特徴とする汚水あるいは汚泥処
理装置。4. An anaerobic tank is provided before the aerobic tank, and a separation membrane for deriving treated water is immersed in the aerobic tank, and a separation membrane for obtaining phosphorus-containing separated water is immersed in the anaerobic tank. A sewage or sludge treatment device is provided with a chemical treatment device for removing phosphorus from the phosphorus-containing separated water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29667991A JP3150734B2 (en) | 1991-10-17 | 1991-10-17 | Wastewater or sludge treatment method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29667991A JP3150734B2 (en) | 1991-10-17 | 1991-10-17 | Wastewater or sludge treatment method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05104090A true JPH05104090A (en) | 1993-04-27 |
| JP3150734B2 JP3150734B2 (en) | 2001-03-26 |
Family
ID=17836677
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP29667991A Expired - Fee Related JP3150734B2 (en) | 1991-10-17 | 1991-10-17 | Wastewater or sludge treatment method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3150734B2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH091188A (en) * | 1995-06-20 | 1997-01-07 | Toto Ltd | Waste water treating device and its operating method |
| WO2001005715A1 (en) * | 1999-07-20 | 2001-01-25 | Zenon Environmental Inc. | Biological process for removing phosphorus involving a membrane filter |
| US6485645B1 (en) | 1999-07-20 | 2002-11-26 | Zenon Environmental Inc | Biological process for removing phosphorus involving a membrane filter |
| WO2008037429A1 (en) * | 2006-09-25 | 2008-04-03 | Finrone Limited | A method and apparatus for the treatment of organic slurry |
| JP4647814B2 (en) * | 2001-03-27 | 2011-03-09 | 住友重機械エンバイロメント株式会社 | Organic wastewater treatment equipment |
| JP2011067727A (en) * | 2009-09-24 | 2011-04-07 | Sumiju Kankyo Engineering Kk | Method and apparatus for treating wastewater |
-
1991
- 1991-10-17 JP JP29667991A patent/JP3150734B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH091188A (en) * | 1995-06-20 | 1997-01-07 | Toto Ltd | Waste water treating device and its operating method |
| WO2001005715A1 (en) * | 1999-07-20 | 2001-01-25 | Zenon Environmental Inc. | Biological process for removing phosphorus involving a membrane filter |
| US6406629B1 (en) | 1999-07-20 | 2002-06-18 | Zenon Environmental Inc. | Biological process for removing phosphorous involving a membrane filter |
| US6485645B1 (en) | 1999-07-20 | 2002-11-26 | Zenon Environmental Inc | Biological process for removing phosphorus involving a membrane filter |
| JP4647814B2 (en) * | 2001-03-27 | 2011-03-09 | 住友重機械エンバイロメント株式会社 | Organic wastewater treatment equipment |
| WO2008037429A1 (en) * | 2006-09-25 | 2008-04-03 | Finrone Limited | A method and apparatus for the treatment of organic slurry |
| JP2011067727A (en) * | 2009-09-24 | 2011-04-07 | Sumiju Kankyo Engineering Kk | Method and apparatus for treating wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3150734B2 (en) | 2001-03-26 |
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