JPH0788500A - Method for treating sewage countercurrent water - Google Patents
Method for treating sewage countercurrent waterInfo
- Publication number
- JPH0788500A JPH0788500A JP5238279A JP23827993A JPH0788500A JP H0788500 A JPH0788500 A JP H0788500A JP 5238279 A JP5238279 A JP 5238279A JP 23827993 A JP23827993 A JP 23827993A JP H0788500 A JPH0788500 A JP H0788500A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- sludge
- water
- sewage
- nitrification
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 239000010865 sewage Substances 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000010802 sludge Substances 0.000 claims abstract description 35
- 238000005273 aeration Methods 0.000 claims abstract description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000006228 supernatant Substances 0.000 claims abstract description 14
- 238000004062 sedimentation Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 7
- 238000005345 coagulation Methods 0.000 claims abstract description 6
- 230000015271 coagulation Effects 0.000 claims abstract description 6
- 150000003018 phosphorus compounds Chemical class 0.000 claims abstract description 4
- 239000005416 organic matter Substances 0.000 claims description 6
- 230000001546 nitrifying effect Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 229920000642 polymer Polymers 0.000 claims description 3
- 230000006641 stabilisation Effects 0.000 abstract description 15
- 238000011105 stabilization Methods 0.000 abstract description 15
- 239000000701 coagulant Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 abstract description 7
- 229910052567 struvite Inorganic materials 0.000 abstract description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 abstract 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 abstract 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 abstract 2
- 229910021529 ammonia Inorganic materials 0.000 abstract 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 abstract 1
- 239000000920 calcium hydroxide Substances 0.000 abstract 1
- 235000011116 calcium hydroxide Nutrition 0.000 abstract 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 abstract 1
- 229910001629 magnesium chloride Inorganic materials 0.000 abstract 1
- 235000011147 magnesium chloride Nutrition 0.000 abstract 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 abstract 1
- 239000000347 magnesium hydroxide Substances 0.000 abstract 1
- 235000012254 magnesium hydroxide Nutrition 0.000 abstract 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 abstract 1
- 235000012245 magnesium oxide Nutrition 0.000 abstract 1
- 239000000395 magnesium oxide Substances 0.000 abstract 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 abstract 1
- 235000019341 magnesium sulphate Nutrition 0.000 abstract 1
- 239000000203 mixture Substances 0.000 abstract 1
- 150000002894 organic compounds Chemical class 0.000 abstract 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 12
- 229910052698 phosphorus Inorganic materials 0.000 description 12
- 239000011574 phosphorus Substances 0.000 description 12
- 230000001112 coagulating effect Effects 0.000 description 6
- 238000001556 precipitation Methods 0.000 description 6
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000005189 flocculation Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 3
- 239000010801 sewage sludge Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000006114 decarboxylation reaction Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、下水処理場、特に下水
汚泥のみを処理する汚泥処理場から発生する下水返流水
の処理方法に関するものである。なお下水返流水には高
濃度系として汚泥濃縮上澄水と脱水ろ液があり、低濃度
系として焼却炉洗水排水があるが、本発明では高濃度系
の下水返流水を対象とするものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating sewage return water generated from a sewage treatment plant, particularly a sludge treatment plant for treating only sewage sludge. The sewage return water includes sludge concentrated supernatant water and dehydrated filtrate as high-concentration systems, and incinerator wash water drainage as low-concentration systems, but the present invention is intended for high-concentration sewage return water. is there.
【０００２】[0002]
【従来の技術】従来の下水処理場では、そこで発生する
下水汚泥を同一処理場内で処理していたので、汚泥処理
に伴って発生する下水返流水は流入する下水と一括処理
することが可能であった。ところが、最近になって下水
汚泥のみを処理する汚泥処理場が建設されるようにな
り、下水返流水のみを処理する設備が必要となってき
た。2. Description of the Related Art In conventional sewage treatment plants, sewage sludge generated there is treated in the same treatment plant, so sewage return water generated by sludge treatment can be treated together with inflowing sewage. there were. However, recently, a sludge treatment plant for treating only sewage sludge has been constructed, and a facility for treating only sewage return water has become necessary.
【０００３】一般にこのような下水返流水は、図７に示
すように凝集沈殿処理→硝化液循環法による硝化脱窒に
より処理されている。この図７において、51は凝集沈殿
槽、52は脱窒槽、53は硝化槽、54は固液分離槽である。
しかし下水返流水中には溶解性物質が多いために前段の
凝集沈殿処理で有機物の多くを除去することができず、
硝化液循環法で除去する必要があるために硝化液循環法
の処理設備が大きくなる欠点があった。また、リン除去
のために凝集沈殿処理で加えたＰＡＣ、塩化第二鉄等の
無機凝集剤によってアルカリ度が消費されるため、硝化
液循環法による硝化・脱窒処理に際して多量のアルカリ
度の補給が必要であった。更にリン除去に要する無機凝
集剤も多量となり、処理コストを増大させる要因となっ
ていた。Generally, such sewage return water is treated by nitrifying and denitrifying by a coagulating sedimentation treatment → nitrifying solution circulation method as shown in FIG. In FIG. 7, 51 is a coagulating sedimentation tank, 52 is a denitrification tank, 53 is a nitrification tank, and 54 is a solid-liquid separation tank.
However, since there are many soluble substances in the sewage return water, most of the organic substances cannot be removed by the coagulation-sedimentation treatment in the previous stage,
Since it needs to be removed by the nitrification solution circulation method, there is a drawback that the processing equipment of the nitrification solution circulation method becomes large. In addition, since the alkalinity is consumed by the inorganic coagulant such as PAC and ferric chloride added in the coagulation-sedimentation process for phosphorus removal, a large amount of alkalinity is replenished during the nitrification / denitrification process by the nitrification solution circulation method. Was needed. Furthermore, the amount of inorganic coagulant required for phosphorus removal is large, which has been a factor of increasing the processing cost.
【０００４】[0004]
【発明が解決しようとする課題】本発明は上記した従来
の問題点を解決して、硝化液循環法の処理設備をコンパ
クト化することができ、またその際のアルカリ度の補給
を削減することができ、更に無機凝集剤の使用量を減少
させて処理コストの引下げを図ることもできる下水返流
水の処理方法を提供するためになされたものである。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned problems of the prior art, can make the treatment equipment of the nitrification solution circulation method compact, and reduce the replenishment of alkalinity at that time. The present invention was made to provide a method for treating sewage return water, which can reduce the treatment cost by reducing the amount of the inorganic coagulant used.
【０００５】[0005]
【課題を解決するための手段】上記の課題を解決するた
めになされた本発明の下水返流水の処理方法は、下水返
流水と返送汚泥とを混合し、原水中の有機物、アンモニ
ア性窒素、リン化合物、ＳＳ分を汚泥に吸着・摂取させ
た後、固液分離して汚泥の一部を曝気して返送汚泥とす
るとともに、上澄水は曝気した後にMg++を添加して反応
させたうえ高分子凝集剤を添加して凝集沈殿処理を行
い、その凝集上澄水を硝化液循環法によって硝化脱窒す
ることを特徴とするものである。The method for treating sewage return water according to the present invention made to solve the above-mentioned problems comprises mixing sewage return water and return sludge to produce organic matter in raw water, ammoniacal nitrogen, After adsorbing and ingesting phosphorus compounds and SS in sludge, solid-liquid separation is performed to aerate part of the sludge to make it into returning sludge, and supernatant water is aerated and then reacted by adding Mg ++ In addition, a polymer flocculant is added to carry out coagulation-precipitation treatment, and the coagulation supernatant water is nitrified and denitrified by a nitrification solution circulation method.
【０００６】[0006]
【作用】本発明の下水返流水の処理方法は、凝集沈殿処
理の前段に原水中の有機物、アンモニア性窒素、リン化
合物、ＳＳ分を汚泥に吸着・摂取させる接触安定化処理
を行うので、凝集沈殿処理の際の凝集剤の削減を図るこ
とができ、併せて無機凝集剤により消費されるアルカリ
度を抑制することができる。また、接触安定化処理によ
って溶解性物質をできるだけ除去し、硝化液循環法の処
理設備のコンパクト化を図ることができる。更に接触安
定化処理の上澄水を曝気することにより脱炭酸によるpH
上昇を図り、硝化液循環法の際のアルカリ度補給を削減
することができる。なお、従来のＰＡＣ、塩化第二鉄等
の無機凝集剤に替えて、MgOまたはMg(OH)2 を使用すれ
ば、リンの他にアンモニア性窒素の一部も除去すること
ができると同時に、硝化脱窒の際のアルカリ度補給も兼
ねることができる。The sewage return water treatment method of the present invention performs a contact stabilization treatment in which sludge absorbs and ingests organic matter, ammoniacal nitrogen, phosphorus compounds, and SS in raw water before the flocculation and precipitation treatment. It is possible to reduce the amount of coagulant used during the precipitation treatment and, at the same time, suppress the alkalinity consumed by the inorganic coagulant. In addition, the contact stabilization treatment removes as much of the soluble substance as possible, and the treatment equipment of the nitrification solution circulation method can be made compact. Furthermore, by aerating the supernatant water of the contact stabilization treatment,
By increasing the temperature, it is possible to reduce the alkalinity replenishment during the nitrification solution circulation method. If MgO or Mg (OH) 2 is used instead of the conventional inorganic coagulant such as PAC and ferric chloride, it is possible to remove not only phosphorus but also a part of ammoniacal nitrogen. It can also serve as an alkalinity supplement for nitrification and denitrification.
【０００７】[0007]
【実施例】以下に本発明を図１のフローシートに基づい
て更に詳細に説明する。本発明は、接触安定化処理→
曝気処理→Mg++による反応→凝集沈殿処理→硝
化脱窒処理の５つのプロセスから構成されるものであ
る。図１のフローシートにおいて、１は接触安定化槽、
２は第１沈殿槽、３は汚泥曝気槽であり、以上の装置に
よりの接触安定化処理が行われる。４は第１沈殿槽２
の上澄水を曝気する曝気槽であり、の曝気処理が行わ
れる。５は反応槽であり、のMg++による反応が行われ
る。６は凝集沈殿槽であり、の凝集沈殿処理が行われ
る。７は脱窒槽、８は硝化槽、９は第２沈殿槽であり、
以上の装置によりの硝化脱窒処理が行われる。The present invention will be described in more detail below with reference to the flow sheet of FIG. The present invention is a contact stabilization treatment →
It consists of five processes: aeration treatment → Mg ++ reaction → coagulation sedimentation treatment → nitrification denitrification treatment. In the flow sheet of FIG. 1, 1 is a contact stabilizing tank,
Reference numeral 2 is a first settling tank, 3 is a sludge aeration tank, and contact stabilization treatment is performed by the above apparatus. 4 is the first settling tank 2
This is an aeration tank that aerates the supernatant water, and the aeration process is performed. Reference numeral 5 is a reaction vessel in which the reaction with Mg ++ is performed. 6 is a coagulating sedimentation tank, in which the coagulating sedimentation treatment is performed. 7 is a denitrification tank, 8 is a nitrification tank, 9 is a second precipitation tank,
The nitrification denitrification process is performed by the above apparatus.
【０００８】まず下水返流水は、汚泥曝気槽３において
曝気され活性化された返送汚泥と混合されたうえ、接触
安定化槽１に入る。ここで下水返流水中の有機物（有機
酸を含む）、アンモニア性窒素、ＳＳが汚泥に吸着され
る。またこの接触安定化槽１の槽内は曝気されているの
で、汚泥移送中にリンを吐き出した嫌気汚泥を大量に含
む下水返流水は嫌気→好気処理されることとなり、リン
が汚泥中に過剰摂取されて下水返流水中のリンの多くが
除去される。First, the sewage return water is mixed with the return sludge that has been aerated and activated in the sludge aeration tank 3, and then enters the contact stabilization tank 1. Here, organic matter (including organic acid), ammoniacal nitrogen, and SS in the sewage return water are adsorbed by the sludge. Further, since the inside of the contact stabilization tank 1 is aerated, the sewage return water containing a large amount of anaerobic sludge that spews phosphorus during sludge transfer is anaerobically → aerobically treated, and phosphorus is contained in the sludge. Excessive intake removes much of the phosphorus in the sewage return water.
【０００９】接触安定化槽１における曝気時間は図２に
示すように通常１〜３時間であり、１時間よりも短いと
リンの除去率が悪く、３時間以上曝気してもリンの除去
率は向上しない。また、接触安定化槽１から流出した下
水返流水は第１沈殿槽２で固液分離され、汚泥の一部は
余剰汚泥として引き抜かれるとともに、汚泥の残部は汚
泥曝気槽３で曝気されて返送汚泥となるが、この汚泥曝
気槽３の曝気時間は図３に示されるように４〜８時間と
する。この曝気時間が４時間よりも短いと、返送汚泥の
吸着量が減少してＢＯＤ除去率が低下する。なお、この
接触安定化処理工程においては有機酸除去によるpH上昇
も行われ、これによって後段の硝化脱窒プロセスのコン
パクト化と、MgO またはMg(OH)2 添加量の削減を図るこ
とができる。The aeration time in the contact stabilization tank 1 is usually 1 to 3 hours as shown in FIG. 2. If it is shorter than 1 hour, the phosphorus removal rate is poor, and even if aeration is performed for 3 hours or more, the phosphorus removal rate is low. Does not improve. Further, the sewage return water flowing out from the contact stabilization tank 1 is subjected to solid-liquid separation in the first settling tank 2, a part of the sludge is extracted as excess sludge, and the rest of the sludge is aerated in the sludge aeration tank 3 and returned. Although it becomes sludge, the aeration time of the sludge aeration tank 3 is 4 to 8 hours as shown in FIG. If the aeration time is shorter than 4 hours, the amount of the returned sludge adsorbed decreases and the BOD removal rate decreases. In addition, in this contact stabilization treatment step, the pH is increased by removing the organic acid, which makes it possible to make the nitrification denitrification process in the latter stage compact and reduce the amount of MgO or Mg (OH) 2 added.
【００１０】第１沈殿槽２の上澄水は次に曝気槽４に入
り、曝気される。これは接触安定化処理工程において上
昇したpHを曝気による脱炭酸によって更に向上させ、ア
ルカリ度添加量の削減を図るとともに、次工程のストラ
バイト生成に必要な８以上のpHとするためである。この
曝気時間はpHによって異なるが、図４に示すように10〜
60分とすればよい。The supernatant water of the first settling tank 2 then enters the aeration tank 4 and is aerated. This is because the pH raised in the contact stabilization treatment step is further improved by decarboxylation by aeration, the amount of alkalinity added is reduced, and the pH is set to 8 or more necessary for the struvite production in the next step. This aeration time varies depending on pH, but as shown in FIG.
It should be 60 minutes.
【００１１】次に反応槽５においてMg++が添加され、１
〜５分間で次の反応が促進され、ストラバイトの結晶が
生成される。 Mg++＋NH4 + ＋PO4 --- → NH4・Mg・PO4 添加されるMg++は通常MgSO4 、MgCl2 が使用されるが、
後段の硝化脱窒のためにはMgO またはMg(OH)2 の方がよ
い。これはアルカリ度補給と兼用できるためである。添
加量は図５に示すように、PO4 --- １モルに対してMgSO
4 、MgCl2 では0.8 〜２モル、MgO またはMg(OH)2 では
２〜４モルがよい。また反応時間は図６に示すように、
MgSO4 、MgCl2 では１〜３分、MgO またはMg(OH)2 では
３〜５分がよい。このストラバイトの結晶の生成によ
り、下水返流水中のリンとアンモニア性窒素の一部が除
去される。また、ここでMg++だけではなく、リン除去と
アルカリ度補給を目的としてCa(OH)2 も併用できる。こ
れはMg++のうち、MgSO4 、MgCl2 といったアルカリ度の
ないMg++と併用するときに特に有効である。Next, in the reaction vessel 5, Mg ++ was added, and 1
The next reaction is promoted in ˜5 minutes to form crystals of struvite. Mg ++ ＋ NH 4 + ＋ PO 4 --- → NH 4・ Mg ・ PO 4 Mg ++ added is usually MgSO 4 or MgCl 2 ,
For later nitrification and denitrification, MgO or Mg (OH) 2 is better. This is because it can also be used as alkalinity replenishment. As shown in FIG. 5, the addition amount is MgSO 4 per 1 mol of PO 4 ---
4 , MgCl 2 is 0.8 to 2 mol, and MgO or Mg (OH) 2 is 2 to 4 mol. The reaction time is as shown in FIG.
MgSO 4 and MgCl 2 are preferably 1 to 3 minutes, and MgO or Mg (OH) 2 is 3 to 5 minutes. The formation of the struvite crystals removes some of the phosphorus and ammoniacal nitrogen in the sewage return water. Further, not only Mg ++ but also Ca (OH) 2 can be used here for the purpose of phosphorus removal and alkalinity supplementation. This of Mg ++, is particularly effective when used in combination with MgSO 4, no alkalinity such MgCl 2 Mg ++.
【００１２】このようにしてストラバイトが生成した
ら、次に凝集沈殿槽６において高分子凝集剤が添加さ
れ、常法により凝集沈殿処理が行われる。ここで凝集剤
としてＰＡＣや塩化第２鉄のような無機凝集剤を使用し
ないのは、ここまでの接触安定化処理とストラバイト生
成によりリンのほとんどが除去または不溶化されている
ことと、無機凝集剤の添加がアルカリ度低下の原因とな
るためである。凝集沈殿したストラバイトは凝集汚泥と
して排出される。After the struvite is produced in this way, a polymer flocculant is then added in the flocculation / sedimentation tank 6, and the flocculation / precipitation treatment is performed by a conventional method. Inorganic coagulants such as PAC and ferric chloride are not used as coagulants because most of phosphorus is removed or insolubilized by the contact stabilization treatment and struvite formation up to this point, and the inorganic coagulants are used. This is because the addition of the agent causes a decrease in alkalinity. The coagulated sedimented struvite is discharged as coagulated sludge.
【００１３】凝集沈殿槽６の上澄水は、脱窒槽７と硝化
槽８による硝化液循環法によって有機物とＳＳが除去さ
れるとともに、硝化脱窒される。ここにおける脱窒槽７
と硝化槽８は通常の活性汚泥のみによる処理でもよい
が、設置面積を考慮すると担体を投入した流動床方式が
好ましい。ただ、凝集沈殿槽６の上澄水にはかなりの有
機分が含まれているので生物の発生量が多く、固定床に
よる生物膜ろ過方式では多量の逆洗水を必要とし、処理
水の回収率が低くなるので好ましくない。最後に第２沈
殿槽９において固液分離が行われ、硝化脱窒汚泥の一部
は硝化脱窒返送汚泥として凝集沈殿槽６の上澄水に添加
され、残部は系外に引き抜かれる。またその上澄水は処
理水として排出される。The supernatant water of the coagulating sedimentation tank 6 is nitrified and denitrified while the organic matter and SS are removed by a nitrification liquid circulation method using a denitrification tank 7 and a nitrification tank 8. Denitrification tank 7 here
The nitrification tank 8 may be treated with only ordinary activated sludge, but a fluidized bed system in which a carrier is charged is preferable in consideration of the installation area. However, since the supernatant water of the coagulation-sedimentation tank 6 contains a considerable amount of organic matter, a large amount of organisms are generated, and a large amount of backwash water is required in the fixed bed biofilm filtration method, and the recovery rate of treated water is high. Is low, which is not preferable. Finally, solid-liquid separation is performed in the second settling tank 9, part of the nitrifying denitrifying sludge is added to the supernatant water of the coagulating settling tank 6 as nitrifying denitrifying return sludge, and the rest is drawn out of the system. Moreover, the supernatant water is discharged as treated water.
【００１４】次に、本発明の方法と従来法により同一の
下水返流水を処理した結果を表１、表２に示す。処理量
は１m3/Hr である。The results of treating the same sewage return water by the method of the present invention and the conventional method are shown in Tables 1 and 2. The throughput is 1 m 3 / Hr.
【表１】 [Table 1]
【００１５】[0015]
【表２】 [Table 2]
【００１６】[0016]
【発明の効果】以上に詳細に説明したように、本発明の
下水返流水の処理方法によれば、硝化液循環法の処理設
備をコンパクト化することができ、アルカリ度の補給を
削減することができ、無機凝集剤の使用量を減少させ処
理コストの引下げを図ることができる。よって本発明
は、高濃度系の下水返流水を省面積的にかつ経済的に処
理するに適した下水返流水の処理方法として、価値の大
きいものである。As described above in detail, according to the sewage return water treatment method of the present invention, the treatment equipment of the nitrification solution circulation method can be made compact and the replenishment of alkalinity can be reduced. Therefore, the amount of the inorganic coagulant used can be reduced and the processing cost can be reduced. Therefore, the present invention is of great value as a sewage return water treatment method suitable for treating highly concentrated sewage return water in an area-saving and economical manner.
【図１】本発明の実施例を示すフローシートである。FIG. 1 is a flow sheet showing an example of the present invention.
【図２】接触安定化槽の曝気時間とリン除去率との関係
を示すグラフである。FIG. 2 is a graph showing the relationship between the aeration time of the contact stabilization tank and the phosphorus removal rate.
【図３】汚泥曝気槽の曝気時間とＢＯＤ除去率との関係
を示すグラフである。FIG. 3 is a graph showing the relationship between the aeration time of a sludge aeration tank and the BOD removal rate.
【図４】曝気槽の曝気時間と曝気液pHとの関係を示すグ
ラフである。FIG. 4 is a graph showing the relationship between the aeration time of the aeration tank and the pH of the aeration liquid.
【図５】Mg++添加率とＴ−Ｐ除去率との関係を示すグラ
フである。FIG. 5 is a graph showing the relationship between the Mg ++ addition rate and the TP removal rate.
【図６】反応槽反応時間とＴ−Ｐ除去率との関係を示す
グラフである。FIG. 6 is a graph showing the relationship between reaction time in a reaction tank and T-P removal rate.
【図７】従来例のフローシートである。FIG. 7 is a flow sheet of a conventional example.
１ 接触安定化槽、２ 第１沈殿槽、３ 汚泥曝気槽、
４ 曝気槽、５ 反応槽、６ 凝集沈殿槽、７ 脱窒
槽、８ 硝化槽、９ 第２沈殿槽1 contact stabilization tank, 2 first settling tank, 3 sludge aeration tank,
4 aeration tank, 5 reaction tank, 6 coagulation sedimentation tank, 7 denitrification tank, 8 nitrification tank, 9 2nd precipitation tank
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０２Ｆ 9/00 ５０４ Ａ 7446−4Ｄ 1/56 ＺＡＢ Ｅ 9042−4Ｄ 3/34 １０１ Ａ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Office reference number FI technical display location C02F 9/00 504 A 7446-4D 1/56 ZAB E 9042-4D 3/34 101 A
Claims (2)
中の有機物、アンモニア性窒素、リン化合物、ＳＳ分を
汚泥に吸着・摂取させた後、固液分離して汚泥の一部を
曝気して返送汚泥とするとともに、上澄水は曝気した後
にMg++を添加して反応させたうえ高分子凝集剤を添加し
て凝集沈殿処理を行い、その凝集上澄水を硝化液循環法
によって硝化脱窒することを特徴とする下水返流水の処
理方法。1. The sewage return water and the returned sludge are mixed, and organic matter, ammoniacal nitrogen, phosphorus compounds, and SS in the raw water are adsorbed and ingested by the sludge, and then solid-liquid separation is performed to partly remove the sludge. Aeration is performed to return sludge, and the supernatant water is aerated and then reacted by adding Mg ++ and then adding a polymer flocculant for coagulation sedimentation treatment, and the coagulation supernatant water is subjected to the nitrification solution circulation method. A method for treating sewage return water, characterized by nitrifying and denitrifying.
ることを特徴とする請求項１に記載の下水返流水の処理
方法。2. The method for treating sewage return water according to claim 1, wherein the added Mg ++ is MgO or Mg (OH) 2 .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5238279A JP2716348B2 (en) | 1993-09-24 | 1993-09-24 | Sewage return water treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5238279A JP2716348B2 (en) | 1993-09-24 | 1993-09-24 | Sewage return water treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0788500A true JPH0788500A (en) | 1995-04-04 |
| JP2716348B2 JP2716348B2 (en) | 1998-02-18 |
Family
ID=17027831
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5238279A Expired - Fee Related JP2716348B2 (en) | 1993-09-24 | 1993-09-24 | Sewage return water treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2716348B2 (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100329597B1 (en) * | 1999-08-07 | 2002-03-21 | 고병석, 고병산 | Composite disposition method for waste water of high density |
| JP2002172400A (en) * | 2000-12-06 | 2002-06-18 | Unitika Ltd | Method and apparatus for removing nitrogen in sludge return water |
| KR20030033474A (en) * | 2001-10-23 | 2003-05-01 | 대한민국(충북대학교총장) | Purifying process and apparatus for waste-water |
| KR100453484B1 (en) * | 2002-09-30 | 2004-10-15 | (주)이엔바이오21 | Method of wasetwater treatment |
| JP2007007620A (en) * | 2005-07-04 | 2007-01-18 | Fuji Electric Holdings Co Ltd | Nitrogen-containing waste liquid treatment method |
| US20100170845A1 (en) * | 2008-02-01 | 2010-07-08 | Robert Baur | Waste activated sludge phosphorus and magnesium stripping process and struvite production system |
| JP2010253404A (en) * | 2009-04-27 | 2010-11-11 | Ebara Engineering Service Co Ltd | Method and apparatus for denitrification treatment of digested sludge separation liquid |
| CN110498537A (en) * | 2019-09-03 | 2019-11-26 | 瓮福（集团）有限责任公司 | A kind of technique that the phosphorus fluorine sewage containing ammonia nitrogen efficiently removes ammonia nitrogen |
| US10604433B2 (en) | 2017-10-24 | 2020-03-31 | Clean Water Services | Emancipative waste activated sludge stripping to remove internal phosphorus (“eWASSTRIP”) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107032575A (en) * | 2017-03-29 | 2017-08-11 | 中国科学院生态环境研究中心 | Method for sludge treatment |
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1993
- 1993-09-24 JP JP5238279A patent/JP2716348B2/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100329597B1 (en) * | 1999-08-07 | 2002-03-21 | 고병석, 고병산 | Composite disposition method for waste water of high density |
| JP2002172400A (en) * | 2000-12-06 | 2002-06-18 | Unitika Ltd | Method and apparatus for removing nitrogen in sludge return water |
| KR20030033474A (en) * | 2001-10-23 | 2003-05-01 | 대한민국(충북대학교총장) | Purifying process and apparatus for waste-water |
| KR100453484B1 (en) * | 2002-09-30 | 2004-10-15 | (주)이엔바이오21 | Method of wasetwater treatment |
| JP2007007620A (en) * | 2005-07-04 | 2007-01-18 | Fuji Electric Holdings Co Ltd | Nitrogen-containing waste liquid treatment method |
| US20100170845A1 (en) * | 2008-02-01 | 2010-07-08 | Robert Baur | Waste activated sludge phosphorus and magnesium stripping process and struvite production system |
| US8496827B2 (en) * | 2008-02-01 | 2013-07-30 | Clean Water Services | Waste activated sludge phosphorus and magnesium stripping process and struvite production system |
| JP2010253404A (en) * | 2009-04-27 | 2010-11-11 | Ebara Engineering Service Co Ltd | Method and apparatus for denitrification treatment of digested sludge separation liquid |
| US10604433B2 (en) | 2017-10-24 | 2020-03-31 | Clean Water Services | Emancipative waste activated sludge stripping to remove internal phosphorus (“eWASSTRIP”) |
| CN110498537A (en) * | 2019-09-03 | 2019-11-26 | 瓮福（集团）有限责任公司 | A kind of technique that the phosphorus fluorine sewage containing ammonia nitrogen efficiently removes ammonia nitrogen |
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| Publication number | Publication date |
|---|---|
| JP2716348B2 (en) | 1998-02-18 |
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