JP3473328B2 - Biological dephosphorization equipment - Google Patents
Biological dephosphorization equipmentInfo
- Publication number
- JP3473328B2 JP3473328B2 JP16422897A JP16422897A JP3473328B2 JP 3473328 B2 JP3473328 B2 JP 3473328B2 JP 16422897 A JP16422897 A JP 16422897A JP 16422897 A JP16422897 A JP 16422897A JP 3473328 B2 JP3473328 B2 JP 3473328B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- phosphorus
- tank
- map
- liquid
- 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
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)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、排出される余剰汚
泥の量が非常に少ないか或いは余剰汚泥が全く排出され
ない生物脱リン装置であって、リンを効率的に除去する
ことができる生物脱リン装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a biological dephosphorization apparatus that discharges very small amount of surplus sludge or does not discharge surplus sludge at all. Regarding phosphorus equipment.
【０００２】[0002]
【従来の技術】従来、生物処理で発生する余剰汚泥をオ
ゾン処理により可溶化して汚泥量を低減する汚泥減容法
が提案されており（特開平６−２０６０８８号公報、同
７−９６２９７号公報）、この方法を生物処理プロセス
に適用することにより、余剰汚泥が全く発生しないか、
或いは、余剰汚泥の発生量を通常の活性汚泥法の場合よ
り大幅に低減することができる。2. Description of the Related Art Conventionally, a sludge volume reduction method has been proposed in which excess sludge generated by biological treatment is solubilized by ozone treatment to reduce the amount of sludge (JP-A-6-206088 and JP-A-7-96297). Gazette), by applying this method to biological treatment process, whether excess sludge is not generated at all,
Alternatively, the amount of surplus sludge generated can be significantly reduced as compared with the case of a normal activated sludge method.
【０００３】しかし、生物脱リンプロセスに、この汚泥
減容法を適用した場合には、余剰汚泥が系外に排出され
ないか或いはその排出量が少ないために、汚泥内に取り
込んだリンを系外へ全く排出することができないか或い
は排出できてもその排出量が少なくなる。However, when this sludge volume reduction method is applied to the biological dephosphorization process, the excess sludge is not discharged to the outside of the system or the amount of the discharged sludge is small, so that the phosphorus taken into the sludge is discharged to the outside of the system. It cannot be discharged at all, or even if it can be discharged, the amount of discharge becomes small.
【０００４】一方、生物処理槽に凝集剤を添加してリン
を不溶性の塩として除去する方法があるが、この方法に
上記汚泥減容法を適用した場合においても、凝集により
生成したリンを含む不溶性の塩を主成分とする汚泥が系
外に排出されないか或いはその排出量が少ないために、
系内でこの汚泥が濃縮される。そして、リンの不溶性塩
を主成分とする汚泥が濃縮されることにより、オゾンに
よる汚泥減容化効果が著しく低下する。On the other hand, there is a method for removing phosphorus as an insoluble salt by adding a flocculant to the biological treatment tank. Even when the above sludge volume reduction method is applied to this method, phosphorus produced by flocculation is included. Since sludge containing insoluble salt as the main component is not discharged to the outside of the system or the amount of discharge is small,
This sludge is concentrated in the system. Then, the sludge containing the insoluble salt of phosphorus as the main component is concentrated, whereby the sludge volume reduction effect of ozone is significantly reduced.
【０００５】[0005]
【発明が解決しようとする課題】上述の如く、現状にお
いて、生物脱リン法と汚泥減容法との組み合せにより、
汚泥の減容化効果とリン除去効果を共に達成することは
困難であった。As described above, at present, by combining the biological dephosphorization method and the sludge volume reduction method,
It was difficult to achieve both the sludge volume reduction effect and the phosphorus removal effect.
【０００６】本発明は上記従来の問題点を解決し、汚泥
の減容化が可能でしかもリンの除去効率に優れる生物脱
リン装置を提供することを目的とする。An object of the present invention is to solve the above-mentioned conventional problems and to provide a biological dephosphorization apparatus capable of reducing the volume of sludge and having excellent phosphorus removal efficiency.
【０００７】[0007]
【課題を解決するための手段】本発明の生物脱リン装置
は、嫌気好気法による生物脱リン装置において、返送汚
泥の一部が導入される汚泥可溶化手段と、該汚泥可溶化
手段で可溶化された汚泥の一部を嫌気槽に返送する手段
と、返送汚泥の一部が導入されるリン放出槽と、前記汚
泥可溶化手段で可溶化された汚泥の他の一部を前記リン
放出槽に移送する手段と、前記リン放出槽の流出液が導
入されるＭＡＰ（リン酸マグネシウムアンモニウム）反
応塔であって、液中のリン及びアンモニアとマグネシウ
ムとの反応でＭＡＰが生成、析出し、これにより、液中
のリンが除去されるように、アルカリを添加してｐＨ
７．５〜１０に調整して１０〜６０分滞留させ、リン濃
度５〜２０ｍｇ／Ｌの流出液を得ると共にＭＡＰ粒子を
回収するための、流動床又は固定床型式のＭＡＰ反応塔
とを備えてなることを特徴とする。A biological dephosphorization apparatus of the present invention is a biological dephosphorization apparatus by an anaerobic aerobic method, which comprises sludge solubilizing means into which a part of returned sludge is introduced and sludge solubilizing means. Means for returning a part of the solubilized sludge to the anaerobic tank, a phosphorus release tank into which a part of the returned sludge is introduced, and another part of the sludge solubilized by the sludge solubilizing means for the phosphorus And a MAP (magnesium ammonium phosphate) reaction tower into which the effluent of the phosphorus release tank is introduced, and the means for transferring to the release tank, wherein phosphorus and ammonia in the solution and magnesium
MAP is produced and precipitated by the reaction with the
PH is adjusted by adding alkali to remove phosphorus
Adjust to 7.5 to 10 and let it stay for 10 to 60 minutes.
5-20 mg / L of effluent and MAP particles
A fluidized bed or fixed bed type MAP reaction column for recovery is provided.
【０００８】本発明の生物脱リン装置では、返送汚泥の
一部を可溶化して再び生物処理することにより、汚泥を
減容化することができる。また、返送汚泥の一部からリ
ン放出槽で放出させたリンをＭＡＰ反応塔でＭＡＰとし
て除去、回収することにより、リンを系外へ排出するこ
とができる。In the biological dephosphorization apparatus of the present invention, the sludge can be reduced in volume by solubilizing a part of the returned sludge and subjecting it to biological treatment again. Further, phosphorus can be discharged to the outside of the system by removing and collecting the phosphorus released from a part of the returned sludge in the phosphorus release tank as MAP in the MAP reaction tower.
【０００９】[0009]
【発明の実施の形態】以下、図面を参照して本発明の実
施の形態を詳細に説明する。BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.
【００１０】図１は本発明の生物脱リン装置が実施の形
態を示す系統図である。FIG. 1 is a system diagram showing an embodiment of the biological dephosphorization apparatus of the present invention.
【００１１】図１の生物脱リン装置は、嫌気槽１，脱窒
素槽２，第１好気槽３，第２好気槽４及び沈殿槽５より
なる嫌気好気処理系と、可溶化槽６よりなる返送汚泥の
可溶化系と、リン放出槽７、分離槽８及びＭＡＰ反応塔
９よりなるリン除去系とで構成される。The biological dephosphorization apparatus of FIG. 1 comprises an anaerobic aerobic treatment system comprising an anaerobic tank 1, a denitrification tank 2, a first aerobic tank 3, a second aerobic tank 4 and a precipitation tank 5, and a solubilizing tank. The system comprises a solubilization system for returning sludge, which is composed of 6 and a phosphorus removal system, which is composed of a phosphorus release tank 7, a separation tank 8 and a MAP reaction tower 9.
【００１２】原水は後述の返送汚泥、可溶化汚泥及びＭ
ＡＰ反応塔流出液と共に、嫌気槽１に導入される。嫌気
槽１では、活性汚泥が原水中の有機物を摂取し、また、
汚泥中の正リン酸を液側へ放出する。Raw water is returned sludge, solubilized sludge and M
It is introduced into the anaerobic tank 1 together with the AP reaction tower effluent. In the anaerobic tank 1, activated sludge ingests organic matter in raw water,
Orthophosphoric acid in sludge is released to the liquid side.
【００１３】嫌気処理液は、脱窒素槽２に導入される。
この脱窒素槽２には、後段の第２好気槽４の処理液の一
部が循環液として返送されており、循環液中のＮＯ2 又
はＮＯ3 態窒素の脱窒素が行われる。The anaerobic treatment liquid is introduced into the denitrification tank 2.
A part of the treatment liquid in the second aerobic tank 4 in the subsequent stage is returned to the denitrification tank 2 as a circulating liquid, and the NO 2 or NO 3 state nitrogen in the circulating liquid is denitrified.
【００１４】脱窒素処理液は、第１好気槽３及び第２好
気槽４に順次導入され好気処理される。好気槽３，４で
は、汚泥中に取り込まれた有機物が酸化分解される。ま
た、リンの過剰摂取が行われ、嫌気槽１で汚泥から放出
されたリン及び原水中のリンが汚泥に取り込まれる。通
常の活性汚泥は、汚泥の乾燥重量当り２％程度のリンを
摂取蓄積するが、生物脱リン活性汚泥では５％程度まで
リンを摂取でき、その分リン除去効率が高い。好気槽
３，４ではまた、液中のＮＨ3 態窒素がＮＯ3 又はＮＯ
2 態窒素に酸化される。The denitrification treatment liquid is successively introduced into the first aerobic tank 3 and the second aerobic tank 4 for aerobic treatment. In the aerobic tanks 3 and 4, the organic substances taken into the sludge are oxidatively decomposed. Further, excessive intake of phosphorus is performed, and phosphorus released from the sludge in the anaerobic tank 1 and phosphorus in the raw water are taken into the sludge. Normal activated sludge ingests and accumulates about 2% of phosphorus based on the dry weight of sludge, but biologically dephosphorized activated sludge can ingest up to about 5% of phosphorus, and the phosphorus removal efficiency is high. In the aerobic tanks 3 and 4, the NH 3 state nitrogen in the liquid is NO 3 or NO.
It is oxidized to 2 nitrogen.
【００１５】好気処理液はその一部が循環液として脱窒
素槽２に返送され、残部は、沈殿槽５で固液分離され
る。A part of the aerobic treatment liquid is returned to the denitrification tank 2 as a circulating liquid, and the rest is solid-liquid separated in the precipitation tank 5.
【００１６】沈殿槽５の分離液は、嫌気好気処理でＢＯ
Ｄが除去されると共に脱窒素槽２で窒素が除去され、か
つ、好気槽３，４でリンが汚泥中に取り込まれることに
より除去された、良好な水質の処理水であり、系外へ排
出される。The separated liquid in the settling tank 5 is anaerobically and aerobically treated with BO.
D is removed, nitrogen is removed in the denitrification tank 2, and phosphorus is removed by incorporating phosphorus into sludge in the aerobic tanks 3 and 4, which is treated water of good water quality, and is removed from the system. Is discharged.
【００１７】沈殿槽５の分離汚泥は、その一部が返送汚
泥として直接嫌気槽１に返送される。A part of the separated sludge in the settling tank 5 is directly returned to the anaerobic tank 1 as return sludge.
【００１８】また、分離汚泥の一部は可溶化槽６に導入
され、オゾンガスの吹き込みにより可溶化処理される。
即ち、汚泥はオゾンによりＢＯＤ成分に酸化分解され、
可溶化される。A part of the separated sludge is introduced into the solubilization tank 6 and solubilized by blowing ozone gas.
That is, sludge is oxidatively decomposed into BOD components by ozone,
Solubilized.
【００１９】この可溶化槽６のオゾン処理ガスとして
は、純オゾンの他、オゾン含有空気、オゾン化空気等を
使用することができる。As the ozone treatment gas in the solubilization tank 6, not only pure ozone but also ozone-containing air, ozonized air and the like can be used.
【００２０】可溶化槽６のオゾン注入量は、少ないと汚
泥の可溶化が十分に行われず、多いとコスト面で不利で
ある。通常の場合、オゾン注入量は、可溶化槽６の流入
汚泥量に対するオゾンの割合で０．０３〜０．１ｇ−Ｏ
3 ／ｇ−ＳＳとするのが好ましい。If the ozone injection amount in the solubilization tank 6 is small, the sludge is not sufficiently solubilized, and if it is large, it is disadvantageous in terms of cost. Normally, the ozone injection amount is 0.03 to 0.1 g-O in terms of the ratio of ozone to the amount of sludge flowing into the solubilization tank 6.
3 / g-SS is preferable.
【００２１】なお、このオゾン処理は、ｐＨ５以下で行
うことによりオゾンの使用量を低減することができる。
従って、本発明では、必要に応じて無機酸を添加するこ
とにより可溶化槽６内のｐＨを５以下、特にｐＨ２．０
〜４．０程度に調整してオゾン処理を行うのが好まし
い。このようにｐＨ調整することにより、オゾン注入量
を０．０１〜０．０５ｇ−Ｏ3 ／ｇ−ＳＳまで低減する
ことが可能となる。The amount of ozone used can be reduced by performing the ozone treatment at a pH of 5 or less.
Therefore, in the present invention, the pH in the solubilization tank 6 is set to 5 or less, particularly pH 2.0 by adding an inorganic acid as needed.
It is preferable that the ozone treatment is carried out by adjusting to about 4.0. By thus pH adjustment, it is possible to reduce the ozone injection rate until 0.01~0.05g-O 3 / g-SS .
【００２２】この可溶化槽６の滞留時間は、汚泥がオゾ
ンにより十分に酸化分解を受けて可溶化される時間であ
れば良く、通常の場合、５分〜１．０時間程度である。
可溶化槽６で可溶化処理された汚泥は、嫌気槽１とリン
放出槽７に適量ずつ移送される。The residence time in the solubilization tank 6 may be any time as long as the sludge is sufficiently oxidatively decomposed by ozone to be solubilized, and usually 5 minutes to 1.0 hour.
Sludge solubilized treated with solubilization tank 6 is fed moved by an appropriate amount to the anaerobic tank 1 and phosphorus release tank 7.
【００２３】また、沈殿槽５の分離汚泥の一部は嫌気性
のリン放出槽７に導入される。リン放出槽７に導入され
た汚泥は、嫌気条件下にゆるやかに撹拌されることで、
好気槽３，４で摂取したリンを液側に放出する。Part of the sludge separated in the settling tank 5 is introduced into the anaerobic phosphorus release tank 7. The sludge introduced into the phosphorus release tank 7 is gently stirred under anaerobic conditions,
The phosphorus ingested in the aerobic tanks 3 and 4 is released to the liquid side.
【００２４】このリン放出槽７の滞留時間は、汚泥中の
リンが十分に放出される時間であれば良く、通常の場
合、１０分〜４時間、好ましくは１〜２時間程度とされ
る。The residence time in the phosphorus release tank 7 may be any time as long as the phosphorus in the sludge is sufficiently released, and usually 10 minutes to 4 hours, preferably about 1 to 2 hours.
【００２５】リン放出槽７の流出液は分離槽８で固液分
離され、分離液はＭＡＰ反応塔９に導入される。一方、
分離汚泥は嫌気槽１に返送される。この分離槽８は沈殿
槽であっても良く、膜分離装置であっても良い。また、
ＭＡＰ反応塔の形状によっては固液分離することなく、
汚泥ごとＭＡＰ反応塔に導入しても良い。The effluent of the phosphorus release tank 7 is subjected to solid-liquid separation in the separation tank 8, and the separated liquid is introduced into the MAP reaction tower 9. on the other hand,
The separated sludge is returned to the anaerobic tank 1. The separation tank 8 may be a precipitation tank or a membrane separation device. Also,
Depending on the shape of the MAP reaction tower, solid-liquid separation does not occur,
The sludge as a whole may be introduced into the MAP reaction tower.
【００２６】ＭＡＰ反応塔９では、ＭＡＰが析出するｐ
Ｈ７．５〜１０、好ましくはｐＨ８〜９となるように、
ＮａＯＨ等のアルカリが注入されると共に、ＭＡＰの析
出にマグネシウムが不足する場合には、ＭｇＣｌ２，Ｍ
ｇ（ＯＨ）２等のマグネシウム化合物（マグネシウム化
合物を含有するものであれば良く、海水であっても良
い。）が添加され、液中のリン及びアンモニアとマグネ
シウムとの反応でＭＡＰが生成、析出し、これにより、
液中のリンが除去される。特に、リン放出槽７で放出さ
れたリンは、生物処理を受けることによりＭＡＰの生成
に有利な正リン酸の形態となっており、ＭＡＰ反応塔９
でのＭＡＰ生成反応効率が高く、このため、効率的なリ
ンの除去を行える。[0026] In the MAP reaction tower 9, MAP is you deposited p
H7.5~10, good Mashiku is in such a way that pH8~9,
When alkali such as NaOH is injected and magnesium is insufficient for MAP precipitation, MgCl 2 , M
Magnesium compound such as g (OH) 2 (as long as it contains a magnesium compound, seawater may be used) is added, and MAP is produced and precipitated by the reaction of phosphorus and ammonia in the liquid with magnesium. And this
Phosphorus in the liquid is removed. In particular, the phosphorus released in the phosphorus release tank 7 is in the form of orthophosphoric acid, which is advantageous for the production of MAP when it is subjected to biological treatment.
The reaction efficiency of MAP production is high, and therefore phosphorus can be efficiently removed.
【００２７】ＭＡＰ反応塔９の流出液はリン濃度５〜２
０ｍｇ／Ｌであり、これをそのまま放流することはでき
ないため、嫌気槽１に返送して処理する。[0027] The effluent of the MAP reaction tower 9 is re-emission concentration 5-2
Since it is 0 mg / L and cannot be discharged as it is, it is returned to the anaerobic tank 1 for processing.
【００２８】なお、ＭＡＰ反応塔９の滞留時間は、１０
〜６０分であり、これにより粒径１〜３ｍｍ程度のＭＡ
Ｐ粒子を回収することができる。このＭＡＰ粒子はリン
及び窒素を含む肥料として有効利用することができる。The residence time in the MAP reaction tower 9 is 10
~ 60 minutes , which results in an MA with a particle size of about 1-3 mm
P particles can be recovered. The MAP particles can be effectively used as a fertilizer containing phosphorus and nitrogen.
【００２９】このような本発明の生物脱リン装置では、
嫌気好気処理系、汚泥可溶化系、リン除去系の処理条件
や汚泥可溶化系への供給汚泥、リン除去系への供給汚泥
を適宜調整することにより、余剰汚泥を全く排出させる
ことなく、リンの効率的な除去を行うことができる。In the biological dephosphorization apparatus of the present invention as described above,
Anaerobic and aerobic treatment system, sludge solubilization system, phosphorus removal system treatment conditions and sludge solubilization system supply sludge, by appropriately adjusting the phosphorus removal system supply sludge, without discharging excess sludge at all, Efficient removal of phosphorus can be performed.
【００３０】なお、図１に示す生物脱リン装置は本発明
の実施の形態の一例であって、本発明はその要旨を超え
ない限り、何ら図示のものに限定されるものではない。The biological dephosphorization apparatus shown in FIG. 1 is an example of the embodiment of the present invention, and the present invention is not limited to the illustrated apparatus as long as the gist thereof is not exceeded.
【００３１】例えば、嫌気槽と好気槽を備えるものであ
れば良く、脱窒素槽２は必ずしも必要とされない。処理
水中の窒素濃度要求レベルが低い場合には、脱窒素槽２
を省略しても良い。また、好気槽を１槽のみ設けたもの
であっても良い。For example, the denitrification tank 2 is not always required as long as it has an anaerobic tank and an aerobic tank. If the required level of nitrogen concentration in the treated water is low, denitrification tank 2
May be omitted. Alternatively, only one aerobic tank may be provided.
【００３２】また、分離槽８も必ずしも必要とされず、
リン放出槽７の流出液は、そのままＭＡＰ反応塔９に送
給しても良い。Further, the separation tank 8 is not always necessary,
The effluent of the phosphorus release tank 7 may be sent to the MAP reaction tower 9 as it is.
【００３３】リン放出槽７の流出液を固液分離せずにそ
のままＭＡＰ反応塔９に送給する場合、ＭＡＰ反応塔は
流動床型式であることが好ましいが、分離槽８を設け、
固液分離後の分離液をＭＡＰ反応塔９に送給する場合
は、ＭＡＰ反応塔９は固定床、流動床のどちらの型式で
あっても良い。また、通水はプラグフローでも良いし、
反応塔下部から曝気を行う完全混合でも良い。When the effluent of the phosphorus release tank 7 is fed to the MAP reaction tower 9 as it is without solid-liquid separation, the MAP reaction tower is preferably of the fluidized bed type, but the separation tank 8 is provided,
When the separated liquid after solid-liquid separation is fed to the MAP reaction tower 9, the MAP reaction tower 9 may be either a fixed bed type or a fluidized bed type. Also, water flow may be a plug flow,
Complete mixing in which aeration is performed from the lower part of the reaction tower may be used.
【００３４】本発明の生物脱リン装置では、可溶化槽を
設けて汚泥の減容化を行うと共に、リン放出槽及びＭＡ
Ｐ反応塔を用いてリンをＭＡＰ粒子として系外へ除去す
るため、余剰汚泥を全く排出しない、或いは、余剰汚泥
排出量を著しく低減した汚泥減容化処理システムにおい
て、余剰汚泥が排出されないためにリンの除去が行えな
いという従来の不具合を解消して、効率的なリン除去を
行うことができる。In the biological dephosphorization apparatus of the present invention, a solubilization tank is provided to reduce the volume of sludge, and a phosphorus release tank and MA
Since phosphorus is removed from the system as MAP particles using the P reaction tower, excess sludge is not discharged at all, or excess sludge is not discharged in a sludge volume reduction treatment system that significantly reduces the amount of excess sludge discharged. It is possible to eliminate the conventional inconvenience that phosphorus cannot be removed and to efficiently remove phosphorus.
【００３５】[0035]
【実施例】以下に実施例及び比較例を挙げて本発明をよ
り具体的に説明する。EXAMPLES The present invention will be described more specifically with reference to Examples and Comparative Examples below.
【００３６】実施例１
図１に示す本発明の生物脱リン装置により、表１に示す
水質の初沈流出下水の処理を行った。Example 1 The biological dephosphorization apparatus of the present invention shown in FIG. 1 was used to treat the sewage of the first settling outflow having the water quality shown in Table 1.
【００３７】各部の仕様及び運転条件は、下記の通りと
した。The specifications and operating conditions of each part are as follows.
【００３８】嫌気好気処理系
原水（初沈流出下水）量：４０ｍ3 ／日
嫌気槽容量：２．５ｍ3
脱窒素槽容量：２．５ｍ3
第１，第２好気槽容量：各々２．５ｍ3 （計５ｍ3 ）
ＭＬＳＳ濃度：４０００ｍｇ／Ｌ
返送汚泥濃度：８０００ｍｇ／Ｌ
汚泥返送率：１００％（余剰汚泥の排出ゼロ）
循環液量：１２０ｍ3 ／日汚泥可溶化系
可溶化槽容量：０．２ｍ3
可溶化槽滞留時間（ＨＲＴ）：６０分
オゾン（可溶化）処理汚泥量：０．６ｍ3 ／日
オゾン注入率：０．０５ｇ−Ｏ3 ／ｇ−ＳＳ
可溶化槽ｐＨ：５．５リン除去系
リン放出槽容量：０．３３ｍ3
リン放出槽供給汚泥量：４ｍ3 ／日
リン放出槽滞留時間（ＨＲＴ）：２時間
ＭＡＰ反応塔容量：４２Ｌ
ＭＡＰ反応塔流入水量：２ｍ3 ／日
ＭＡＰ反応塔滞留時間（ＨＲＴ）：３０分
ＭＡＰ反応塔ｐＨ：８．７（２Ｎ ＮａＯＨで自動制
御）
ＭＡＰ反応塔 MgCl2添加量：７０ｍｇ／Ｌ（処理水量に
対するＭｇ換算量）
ＭＡＰ反応塔上昇ＬＶ：１００ｍ／時間（循環ポンプに
よる流動床運転）
得られた処理水の水質（３ケ月間連続運転の平均値）及
び返送汚泥中のリン含有率を表１に示した。 Anaerobic / aerobic treatment system Raw water (first settling outflow sewage): 40 m 3 / day Anaerobic tank capacity: 2.5 m 3 Denitrification tank capacity: 2.5 m 3 1st and 2nd aerobic tank capacity: 2 each 0.5 m 3 (total 5 m 3 ) MLSS concentration: 4000 mg / L Return sludge concentration: 8000 mg / L Sludge return rate: 100% (no excess sludge discharge) Circulating liquid amount: 120 m 3 / day Sludge solubilization system capacity : 0.2m 3 solubilization tank retention time (HRT): 60 minutes Ozone (solubilization) treated sludge amount: 0.6m 3 / day Ozone injection rate: 0.05g-O 3 / g-SS Solubilization tank pH: 5.5 Phosphorus removal system Phosphorus release tank capacity: 0.33 m 3 Phosphorus release tank supply sludge amount: 4 m 3 / day Phosphorus release tank retention time (HRT): 2 hours MAP reaction tower capacity: 42 L MAP reaction tower inflow water amount: 2 m 3 / day MAP reactor residence time (HRT): 30 minutes MAP anti Tower pH: 8.7 (2N NaOH automatic control) MAP reactor MgCl 2 amount: 70 mg / L (Mg equivalent amount with respect to the processing water) MAP reactor increased LV: 100 m / Time (fluidized bed operation by the circulating pump) to give Table 1 shows the water quality of the treated water (average value of continuous operation for 3 months) and the phosphorus content in the returned sludge.
【００３９】また、ＭＡＰ反応塔の流入水と流出水の水
質を表２に示した。Table 2 shows the water quality of the inflow water and the outflow water of the MAP reaction tower.
【００４０】比較例１
実施例１において、リン放出槽、分離槽及びＭＡＰ反応
塔よりなるリン除去系統を設けなかったこと以外は、同
様にして処理を行い、得られた処理水の水質及び返送汚
泥中のリン含有率を表１に示した。Comparative Example 1 The same treatment as in Example 1 was carried out except that the phosphorus removal system consisting of the phosphorus release tank, the separation tank and the MAP reaction tower was not provided, and the quality and return of the obtained treated water The phosphorus content in the sludge is shown in Table 1.
【００４１】[0041]
【表１】 [Table 1]
【００４２】[0042]
【表２】 [Table 2]
【００４３】実施例１及び比較例１の結果から次のこと
がわかる。From the results of Example 1 and Comparative Example 1, the following can be seen.
【００４４】即ち、実施例１では、初沈流出下水中のリ
ン（Ｔ−Ｐ）は２．５４ｍｇ／Ｌから０．４４ｍｇ／Ｌ
にまで低減され（リン除去率８３％）、リンが効率的に
除去された。一方、比較例１では、汚泥中のリンは４％
以上になっているが余剰汚泥の引き抜きがないため、処
理水のリン（Ｔ−Ｐ）は２．３８ｍｇ／Ｌでリンは殆ど
除去されなかった。That is, in Example 1, phosphorus (TP) in the first settling outflow sewage was 2.54 mg / L to 0.44 mg / L.
(Phosphorus removal rate was 83%), and phosphorus was efficiently removed. On the other hand, in Comparative Example 1, phosphorus in sludge is 4%.
As described above, since the excess sludge was not extracted, phosphorus (TP) in the treated water was 2.38 mg / L, and phosphorus was hardly removed.
【００４５】なお、ＢＯＤ及び窒素除去率については実
施例１と比較例１では殆ど差はなく、共に良好な結果が
得られた。Regarding the BOD and the nitrogen removal rate, there was almost no difference between Example 1 and Comparative Example 1, and good results were obtained.
【００４６】実施例１において、リン放出槽では汚泥中
のリンが放出され、ＨＲＴ２時間でＰＯ4 −Ｐ６３．５
ｍｇ／Ｌ（ＭＡＰ反応塔流入水のＰＯ4 −Ｐ）となり、
これはＳＳ当りのリン放出割合で約０．８％であった。In Example 1, phosphorus in the sludge was released in the phosphorus release tank, and PO 4 -P63.5 after 2 hours of HRT.
mg / L (PO 4 -P of MAP reaction tower inflow water),
This was about 0.8% in phosphorus release rate per SS.
【００４７】また、実施例１のＭＡＰ反応塔ではＨＲＴ
３０分でＰＯ4 −Ｐ６３．５ｍｇ／Ｌから１３．４ｍｇ
／Ｌにまで効率的にリンが除去され、リンの除去率は７
９％であった。In the MAP reaction tower of Example 1, HRT was used.
From PO 4 -P 63.5 mg / L to 13.4 mg in 30 minutes
/ L is efficiently removed, and the removal rate of phosphorus is 7
It was 9%.
【００４８】なお、実施例１及び比較例１では余剰汚泥
の引き抜きを全く行わないで運転を行ったが、可溶化槽
を設けず汚泥の減容化を行わなかった場合に発生する推
定余剰汚泥量（処理水量×除去ＳＳ濃度×１．０）はい
ずれの場合も、約１．４ｋｇ−乾燥ＳＳ／日であり、汚
泥の減容化効果については、実施例１も比較例１も同等
の効果が得られた。In addition, in Example 1 and Comparative Example 1, the operation was performed without extracting the excess sludge, but the estimated excess sludge generated when the volume of the sludge was not reduced without providing the solubilizing tank. The amount (treated water amount × removed SS concentration × 1.0) was about 1.4 kg-dry SS / day in each case, and the volume reduction effect of sludge was the same in both Example 1 and Comparative Example 1. The effect was obtained.
【００４９】[0049]
【発明の効果】以上詳述した通り、本発明の生物脱リン
装置によれば、汚泥を減容化して系外への余剰汚泥の排
出を全く行わないか或いは余剰汚泥の排出量を著しく低
減できると共に、リンを効率的に除去してＭＡＰ粒子と
して回収することができる。As described in detail above, according to the biological dephosphorization apparatus of the present invention, the volume of sludge is reduced so that excess sludge is not discharged to the outside of the system, or the amount of excess sludge discharged is significantly reduced. At the same time, phosphorus can be efficiently removed and recovered as MAP particles.
【図１】本発明の生物脱リン装置の実施の形態を示す系
統図である。FIG. 1 is a system diagram showing an embodiment of a biological dephosphorization apparatus of the present invention.
１ 嫌気槽 ２ 脱窒素槽 ３ 第１好気槽 ４ 第２好気槽 ５ 沈殿槽 ６ 可溶化槽 ７ リン放出槽 ８ 分離槽 ９ ＭＡＰ反応塔 1 Anaerobic tank 2 denitrification tank 3 First aerobic tank 4 Second aerobic tank 5 settling tank 6 Solubilization tank 7 Phosphorus release tank 8 separation tanks 9 MAP reaction tower
───────────────────────────────────────────────────── フロントページの続き (72)発明者 竹内 忠雄 東京都新宿区西新宿３丁目４番７号 栗 田工業株式会社内 (56)参考文献 特開 平10−490（ＪＰ，Ａ) 特開 平８−39096（ＪＰ，Ａ) 特開 平10−15585（ＪＰ，Ａ) 特開 平９−122678（ＪＰ，Ａ) 特開 平１−119392（ＪＰ，Ａ) 特開 平８−290171（ＪＰ，Ａ) 特開 昭64−4295（ＪＰ，Ａ) 橋本 奨、他６名，新しい活性汚泥法 第４版，日本，産業用水調査会，1997 年 ４月，第４版，56−58 (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 3/28 - 3/34 C02F 3/12 C02F 1/58 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Tadao Takeuchi 3-4-7 Nishishinjuku, Shinjuku-ku, Tokyo Kurita Industry Co., Ltd. (56) Reference JP-A-10-490 (JP, A) JP JP-A-8-39096 (JP, A) JP-A-10-15585 (JP, A) JP-A-9-122678 (JP, A) JP-A-1-119392 (JP, A) JP-A-8-290171 (JP , A) JP 64-4295 (JP, A) Hashimoto Shou, 6 others, new activated sludge method 4th edition, Japan, Industrial Water Research Committee, April 1997, 4th edition, 56-58 (58) ) Fields surveyed (Int.Cl. 7 , DB name) C02F 3/28-3/34 C02F 3/12 C02F 1/58
Claims (2)
て、返送汚泥の一部が導入される汚泥可溶化手段と、該
汚泥可溶化手段で可溶化された汚泥の一部を嫌気槽に返
送する手段と、返送汚泥の一部が導入されるリン放出槽
と、前記汚泥可溶化手段で可溶化された汚泥の他の一部
を前記リン放出槽に移送する手段と、前記リン放出槽の
流出液が導入されるＭＡＰ反応塔であって、液中のリン
及びアンモニアとマグネシウムとの反応でＭＡＰが生
成、析出し、これにより、液中のリンが除去されるよう
に、アルカリを添加してｐＨ７．５〜１０に調整して１
０〜６０分滞留させ、リン濃度５〜２０ｍｇ／Ｌの流出
液を得ると共にＭＡＰ粒子を回収するための、流動床又
は固定床型式のＭＡＰ反応塔とを備えてなることを特徴
とする生物脱リン装置。1. In a biological dephosphorization apparatus by an anaerobic aerobic method, a sludge solubilizing means into which a part of the returned sludge is introduced, and a part of the sludge solubilized by the sludge solubilizing means are returned to an anaerobic tank. Means, a phosphorus release tank into which a part of the returned sludge is introduced, a means for transferring another part of the sludge solubilized by the sludge solubilizing means to the phosphorus release tank, and a phosphorus release tank A MAP reaction tower into which the effluent is introduced, in which phosphorus
And the reaction of ammonia with magnesium produces MAP
It forms and precipitates so that phosphorus in the liquid is removed.
Then, add alkali to adjust the pH to 7.5-10.
Retain for 0 to 60 minutes and flow out with a phosphorus concentration of 5 to 20 mg / L
A fluidized bed or to obtain liquid and to collect MAP particles
Is a fixed bed type MAP reaction tower and is equipped with a biological dephosphorization apparatus.
出液を固液分離する分離槽と、該分離槽で分離された分
離液を前記ＭＡＰ反応塔に導入する手段とを備えてなる
ことを特徴とする生物脱リン装置。Wherein Oite to claim 1, and a separation tank for solid-liquid separating effluent of said phosphorus release vessel, and means for introducing the separated liquid separated in the separation tank to the MAP reactor consisting <br/> biological dephosphorization and wherein the.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16422897A JP3473328B2 (en) | 1997-06-20 | 1997-06-20 | Biological dephosphorization equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16422897A JP3473328B2 (en) | 1997-06-20 | 1997-06-20 | Biological dephosphorization equipment |
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| Publication Number | Publication Date |
|---|---|
| JPH1110191A JPH1110191A (en) | 1999-01-19 |
| JP3473328B2 true JP3473328B2 (en) | 2003-12-02 |
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| JP4124902B2 (en) * | 1999-03-15 | 2008-07-23 | 前澤工業株式会社 | Wastewater treatment equipment |
| JP2000296399A (en) * | 1999-04-13 | 2000-10-24 | Maezawa Ind Inc | Waste water treating apparatus |
| KR100337758B1 (en) * | 1999-07-29 | 2002-05-24 | 박호군 | Sludge-Free Biological Process For Wastewater Treatment |
| KR20020006909A (en) * | 2000-07-14 | 2002-01-26 | 김형벽ㅂ | Advanced wastewater treatment process with the parallel internal recycle |
| JP2003047988A (en) * | 2001-08-03 | 2003-02-18 | Ebara Corp | Method and apparatus for treating organic polluted water |
| KR100420759B1 (en) * | 2001-11-06 | 2004-03-02 | 박성돈 | Ionized gas aided circulation non-discharge system and method for treating excrements wastewater |
| US6706185B2 (en) | 2002-05-22 | 2004-03-16 | Kurita Water Industries Ltd. | Biological method of phosphorus removal and biological phosphorus-removing apparatus |
| FR2843106B1 (en) * | 2002-08-05 | 2004-10-08 | Omnium Traitement Valorisa | PROCESS AND PLANT FOR TREATING SLUDGE FROM BIOLOGICAL WATER PURIFICATION PLANTS |
| KR100837698B1 (en) | 2007-09-03 | 2008-06-13 | 주식회사 피엠씨코리아 | A device capable of removal the nitrogen, phosphorus and etc. from sludge |
| JP4854706B2 (en) * | 2008-06-09 | 2012-01-18 | 水ｉｎｇ株式会社 | Organic wastewater treatment method and treatment apparatus |
| KR101227556B1 (en) * | 2012-08-23 | 2013-01-29 | 뉴엔텍(주) | High efficiency sludge reduce apparatus |
| KR101227558B1 (en) * | 2012-08-23 | 2013-01-29 | 뉴엔텍(주) | Sludge drawing system of digester |
| CN104591473B (en) * | 2013-11-01 | 2017-04-12 | 中国石油化工股份有限公司大连石油化工研究院 | Advanced nitrogen and phosphorus removal technology |
| CN107216005A (en) * | 2017-07-28 | 2017-09-29 | 湖南科技大学 | The sewage-treatment plant and process of a kind of enhanced biological nitrogen removal chemical dephosphorization |
| CN108585369B (en) * | 2018-05-17 | 2020-07-21 | 王胜军 | Aquaculture base sewage treatment system and treatment method adopting Internet of things technology |
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1997
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Non-Patent Citations (1)
| Title |
|---|
| 橋本 奨、他６名，新しい活性汚泥法 第４版，日本，産業用水調査会，１９９７年 ４月，第４版，５６−５８ |
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