JPH0218155B2 - - Google Patents
Info
- Publication number
- JPH0218155B2 JPH0218155B2 JP4656884A JP4656884A JPH0218155B2 JP H0218155 B2 JPH0218155 B2 JP H0218155B2 JP 4656884 A JP4656884 A JP 4656884A JP 4656884 A JP4656884 A JP 4656884A JP H0218155 B2 JPH0218155 B2 JP H0218155B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- liquid
- anaerobic digestion
- tank
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000010802 sludge Substances 0.000 claims description 41
- 239000007788 liquid Substances 0.000 claims description 27
- 230000029087 digestion Effects 0.000 claims description 20
- 238000000034 method Methods 0.000 claims description 19
- 238000005188 flotation Methods 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 7
- 238000003795 desorption Methods 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 3
- 238000004065 wastewater treatment Methods 0.000 claims 1
- 239000010865 sewage Substances 0.000 description 10
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 6
- 238000005273 aeration Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000008719 thickening Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 241000628997 Flos Species 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000010800 human waste Substances 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 206010013496 Disturbance in attention Diseases 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009300 dissolved air flotation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000001603 reducing effect Effects 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- Y02W10/12—
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、下水、し尿その他の有機性汚水処理
における嫌気性消化脱離液の処理方法に関するも
のである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for treating anaerobic digestion fluid in the treatment of sewage, human waste, and other organic wastewater.
一般に、有機性汚水処理において発生する汚泥
の嫌気性消化脱離液は、最初沈殿池に返送され、
流入原水と混合されて処理されているが、嫌気性
消化脱離液中には多量のリン酸、アンモニア、
BODなどが残留しているため、処理水の水質を
悪化させることが多く、バツクロードトラブルと
呼ばれている。
Generally, the anaerobic digestion solution of sludge generated in organic sewage treatment is first returned to a settling tank,
Although it is mixed with the inflow raw water and treated, the anaerobic digestion and desorption fluid contains large amounts of phosphoric acid, ammonia,
Because BOD and other substances remain, the quality of the treated water often deteriorates, which is called backload trouble.
また、有機性汚水処理において発生する汚泥
は、その処理、処分を容易にするためにできるだ
け濃縮することが必要である。特に有機性汚水処
理の活性汚泥法などの生物処理工程から発生する
余剰汚泥は、きわめて濃縮性が悪いという大きな
問題点があり、単なる沈殿濃縮では高濃度に濃縮
することができないので、遠心濃縮法、加圧溶解
空気による浮上濃縮法が採用されることが多くな
つている。しかしながら、これらの濃縮法は何れ
も多くの機器類を必要とし、さらにこれらの運転
に多大のエネルギを要するという新たな問題を引
き起こしている。 Furthermore, sludge generated in organic sewage treatment needs to be concentrated as much as possible to facilitate its treatment and disposal. In particular, surplus sludge generated from biological treatment processes such as the activated sludge method for organic sewage treatment has a major problem in that it has extremely poor concentration, and cannot be concentrated to a high concentration by simple precipitation concentration, so centrifugal concentration is used. , flotation concentration using pressurized dissolved air is increasingly being adopted. However, all of these concentration methods require a large amount of equipment, and furthermore, their operation requires a large amount of energy, which poses a new problem.
本発明は、前述した嫌気性消化脱離液のバツク
ロードトラブルを解決し、同時にきわめて省エネ
ルギ的に汚泥の浮上濃縮をも有効に行うことがで
きる方法を提供することを目的とするものであ
る。
It is an object of the present invention to provide a method that can solve the above-mentioned backload problem of anaerobic digestion and desorption fluid, and at the same time can effectively carry out flotation and concentration of sludge in an extremely energy-saving manner. .
本発明は、生物処理工程と汚泥の嫌気性消化工
程を含む有機性汚水処理において、該処理におい
て発生する汚泥のうち少なくとも余剰活性汚泥を
前記嫌気性消化工程からの脱離液に混合し、該混
合液を硝化工程に導いて硝化処理し、得られた硝
化混合液を浮上濃縮工程に導いて液中のNOx−
Ｎの脱窒素現象によつて生ずる窒素ガスを用いて
液中の汚泥を浮上濃縮分離することを特徴とする
ものである。
The present invention provides organic sewage treatment including a biological treatment step and a sludge anaerobic digestion step, in which at least surplus activated sludge of the sludge generated in the treatment is mixed with the desorbed liquid from the anaerobic digestion step; The mixed liquid is led to a nitrification process for nitrification treatment, and the resulting nitrified mixed liquid is led to a flotation concentration process to eliminate NOx− in the liquid.
This method is characterized by flotation and concentration separation of sludge in a liquid using nitrogen gas generated by the denitrification phenomenon of N.
本発明の一実施例を図面を参照しながら説明す
れば、有機性汚水１は最初沈殿池２に至つて初沈
汚泥３を沈殿分離したのち、曝気槽４に導かれ、
返送汚泥９と混合されてブロワ５から散気装置６
を経て吹き込まれる空気によつて生物処理され
る。曝気槽４にて生物処理された混合液は、さら
に最終沈殿池７において再び分離され、上澄水は
処理水８として取り出され、分離された汚泥の一
部は返送汚泥９として曝気槽４に返送され、他部
は余剰活性汚泥１０として排出される。
An embodiment of the present invention will be described with reference to the drawings. Organic sewage 1 reaches an initial settling tank 2 where initial settled sludge 3 is separated by sedimentation, and then led to an aeration tank 4.
It is mixed with the return sludge 9 and sent to the air diffuser 6 from the blower 5.
Biological treatment is carried out by the air blown through the air. The mixed liquid subjected to biological treatment in the aeration tank 4 is further separated again in the final settling tank 7, the supernatant water is taken out as treated water 8, and a part of the separated sludge is returned to the aeration tank 4 as return sludge 9. The remaining part is discharged as surplus activated sludge 10.
さらに、最初沈殿池２において分離された初沈
汚泥３は濃縮槽１１にて濃縮され、得られた分離
液１２は前記有機性汚水１と共に最初沈殿池２に
至る一方、濃縮汚泥１３は後述する高濃度のフロ
ス２１と共に嫌気性消化槽１４に導入される。嫌
気性消化槽１４にて消化処理された消化汚泥１５
は、固液分離部１６において嫌気性脱離液１７を
分離して、図示しない汚泥処理工程へ送られる。 Furthermore, the first settling sludge 3 separated in the first settling tank 2 is concentrated in a thickening tank 11, and the obtained separated liquid 12 reaches the first settling tank 2 together with the organic sewage 1, while the thickened sludge 13 will be described later. It is introduced into the anaerobic digestion tank 14 together with the highly concentrated froth 21. Digested sludge 15 digested in anaerobic digestion tank 14
The anaerobic desorbed liquid 17 is separated in the solid-liquid separation section 16 and sent to a sludge treatment process (not shown).
また、嫌気性脱離液１７は、最終沈殿池７で得
られた余剰活性汚泥１０が混合されて硝化槽１８
に導かれ、ブロワ１９にて空気が送給されて曝気
を受け、脱離液１７中のアンモニア性窒素
（NH3−Ｎ）が生物学的に硝化され、またBOD物
質なども酸化される。この場合、余剰活性汚泥１
０中には硝化菌が存在し、しかも脱離液１７の水
温は30℃前後と高いので、硝化反応は効果的に進
行する。しかして、NH3−ＮはNOx−Ｎに酸化
され、混合液は浮上濃縮槽２０に流入する。 In addition, the anaerobic desorption liquid 17 is mixed with excess activated sludge 10 obtained in the final settling tank 7 and is added to the nitrification tank 18.
A blower 19 supplies air and aeration occurs, and ammonia nitrogen (NH 3 --N) in the desorbed liquid 17 is biologically nitrified, and BOD substances and the like are also oxidized. In this case, excess activated sludge 1
Since nitrifying bacteria are present in the 0 and the water temperature of the desorbed liquid 17 is high at around 30°C, the nitrification reaction proceeds effectively. Thus, NH 3 --N is oxidized to NOx --N, and the mixed liquid flows into the flotation concentration tank 20.
この浮上濃縮槽２０においては、NOx−Ｎは
生物学的に脱窒素され、生成したN2ガスが汚泥
フロツク表面や内部に付着する結果、液中の汚泥
分は浮上濃縮されて高濃度のフロス２１となる。
なお、NOx−Ｎの生物学的脱窒素は、内生呼吸
タイプでも十分可能であるが、外部より有機炭素
源を添加してもよい。 In the flotation concentration tank 20, NOx-N is denitrified biologically, and the generated N2 gas adheres to the surface and inside of the sludge floc, and as a result, the sludge in the liquid is floated and concentrated, forming a highly concentrated floc. It will be 21.
Note that biological denitrification of NOx-N is fully possible with an endogenous respiration type, but an organic carbon source may be added from the outside.
本発明者の実験によれば、浮上濃縮槽２０に流
入する混合液のNOx−Ｎが20mg／以上存在す
れば、確実にN2ガスによる浮上分離が生起し、
24時間後にはフロス２１の濃度は4.0〜4.2％に達
することが認められた。 According to the inventor's experiments, if the mixed liquid flowing into the flotation concentration tank 20 contains 20 mg/or more of NOx-N, flotation separation by N2 gas will definitely occur.
After 24 hours, the concentration of Floss 21 was observed to reach 4.0-4.2%.
また、嫌気性消化脱離液１７のNH3−Ｎは、
下水の場合40〜200mg／（平均65mg／）であ
ることが、本発明者による下水処理場の実態調査
で判明しており、このNH3−Ｎが硝化槽１８に
てNOx−Ｎに硝化されるから、浮上濃縮槽２０
に流入するNOx−Ｎは平均65mg／となり、こ
の結果安定した浮上濃縮が進行することが認めら
れた。万一、嫌気性脱離液１７中のNH3−Ｎが
減少した場合には、硝化槽１８にNH3源（し尿
が効果的である）を添加するか又はNOx源を添
加するようにすれば万全である。 In addition, NH 3 −N of the anaerobic digestion desorbed liquid 17 is
In the case of sewage, it has been found through a survey of sewage treatment plants that the concentration is 40 to 200 mg/(average 65 mg/), and this NH3 -N is nitrified to NOx-N in the nitrification tank 18. Therefore, floating concentration tank 20
The amount of NOx-N flowing into the tank was 65mg/on average, and as a result, stable flotation concentration was observed to proceed. In the unlikely event that NH 3 -N in the anaerobic desorbed liquid 17 decreases, add an NH 3 source (human waste is effective) or a NOx source to the nitrification tank 18. All is well.
しかして、高濃度のフロス２１は、初沈汚泥３
の濃縮汚泥１３と共に嫌気性消化槽１４に流入
し、嫌気性消化処理が行われる。 Therefore, the high concentration of floss 21 is the first settled sludge 3.
The sludge flows into the anaerobic digestion tank 14 together with the thickened sludge 13, and is subjected to anaerobic digestion treatment.
かくして、浮上濃縮槽２０から流出する分離液
２２は、BOD、窒素成分及びリン酸が除去され
ており、最初沈殿池２にリサイクルしても、従来
のようにバツクロードトラブルを招くことはな
い。なお、初沈汚泥３は、本来濃縮性が比較的良
好であるため、濃縮槽１１としては重力シツクナ
で十分であるが、この初沈汚泥３を硝化槽１８に
流入させてもよい。 Thus, the separated liquid 22 flowing out from the flotation concentration tank 20 has BOD, nitrogen components, and phosphoric acid removed, and even if it is initially recycled to the sedimentation tank 2, it will not cause backload trouble as in the conventional case. Note that since the initial settling sludge 3 originally has relatively good thickening properties, a gravity thickener is sufficient as the thickening tank 11, but the initial settling sludge 3 may be flowed into the nitrification tank 18.
以上述べたように、本発明は嫌気性消化脱離液
に少なくとも余剰活性汚泥を混合し、生物学的に
嫌気性消化脱離液を浄化するとともに、NH3−
Ｎを硝化して生成せしめたNOx−Ｎの還元作用
によつて、N2ガス気泡を発生させて汚泥を浮上
濃縮させるもので、次のような有益なる効果を有
するものである。
As described above, the present invention mixes at least surplus activated sludge with the anaerobic digestion solution, biologically purifies the anaerobic digestion solution, and removes NH 3 −
This system generates N 2 gas bubbles through the reducing action of NOx-N produced by nitrifying N to float and concentrate sludge, and has the following beneficial effects.
従来、バツクロードトラブルの元凶となつて
いた嫌気性消化脱離液のBOD窒素成分、リン
酸等が除去されるから、バツクロードトラブル
を招かない。 BOD nitrogen components, phosphoric acid, etc. in the anaerobic digestion and desorption fluid, which were the cause of backload troubles in the past, are removed, so backload troubles do not occur.
重力濃縮法では濃度２％以上に濃縮すること
が困難である難濃縮性の余剰活性汚泥でも、安
定して固形物濃度４％以上の濃縮汚泥とするこ
とができ、以後の嫌気性消化工程または汚泥脱
水工程を合理化できる。 Even difficult-to-thicken surplus activated sludge, which is difficult to concentrate to a concentration of 2% or more using the gravity thickening method, can be stably made into thickened sludge with a solids concentration of 4% or more, which can be used in the subsequent anaerobic digestion process or The sludge dewatering process can be streamlined.
従来の遠心濃縮法、加圧溶解空気浮上法のよ
うに多くの機器類を必要とせず、無動力で浮上
濃縮が可能となる。 Unlike conventional centrifugal concentration methods and pressurized dissolved air flotation methods, this method does not require a large amount of equipment and enables flotation concentration without power.
図面は本発明の一実施例を示す系統説明図であ
る。
１……有機性汚水、２……最初沈殿池、３……
初沈汚泥、４……曝気槽、５，１９……ブロワ、
６……散気装置、７……最終沈殿池、８……処理
水、９……返送汚泥、１０……余剰活性汚泥、１
１……濃縮槽、１２……分離液、１３……濃縮汚
泥、１４……嫌気性消化槽、１５……消化汚泥、
１６……固液分離部、１７……嫌気性脱離液、１
８……硝化槽、２０……浮上濃縮槽、２１……フ
ロス、２２……分離液。
The drawing is a system explanatory diagram showing an embodiment of the present invention. 1...Organic sewage, 2...First settling tank, 3...
Initial settling sludge, 4...Aeration tank, 5,19...Blower,
6... Aeration device, 7... Final settling tank, 8... Treated water, 9... Return sludge, 10... Excess activated sludge, 1
1... Thickening tank, 12... Separated liquid, 13... Thickened sludge, 14... Anaerobic digestion tank, 15... Digested sludge,
16... Solid-liquid separation section, 17... Anaerobic desorption liquid, 1
8...Nitrification tank, 20...Flotation concentration tank, 21...Floss, 22...Separated liquid.
Claims (1)
有機性汚水処理において、該処理において発生す
る汚泥のうち少なくとも余剰活性汚泥を前記嫌気
性消化工程からの脱離液に混合し、該混合液を硝
化工程に導いて硝化処理し、得られた硝化混合液
を浮上濃縮工程に導いて液中のNOx−Ｎの脱窒
素現象によつて生ずる窒素ガスを用いて液中の汚
泥を浮上濃縮分離することを特徴とする嫌気性消
化脱離液の処理方法。 ２ 前記硝化工程がNH3源又はNOx源を添加し
て硝化処理するものである特許請求の範囲第１項
記載の嫌気性消化脱離液の処理方法。[Scope of Claims] 1. In an organic wastewater treatment including a biological treatment step and a sludge anaerobic digestion step, at least surplus activated sludge of the sludge generated in the treatment is mixed with the desorbed liquid from the anaerobic digestion step. Then, the mixed liquid is led to a nitrification process for nitrification treatment, and the obtained nitrified mixed liquid is led to a flotation concentration process, where the nitrogen gas generated by the denitrification phenomenon of NOx-N in the liquid is used to remove the nitrogen gas in the liquid. A method for treating anaerobic digestion and desorption fluid, which is characterized by flotation concentration separation of sludge. 2. The method for treating anaerobic digestion and desorption fluid according to claim 1, wherein the nitrification step is performed by adding an NH 3 source or a NOx source.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59046568A JPS60190297A (en) | 1984-03-13 | 1984-03-13 | Treatment of anaerobically digested separated liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59046568A JPS60190297A (en) | 1984-03-13 | 1984-03-13 | Treatment of anaerobically digested separated liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60190297A JPS60190297A (en) | 1985-09-27 |
| JPH0218155B2 true JPH0218155B2 (en) | 1990-04-24 |
Family
ID=12750920
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59046568A Granted JPS60190297A (en) | 1984-03-13 | 1984-03-13 | Treatment of anaerobically digested separated liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60190297A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04148445A (en) * | 1990-10-12 | 1992-05-21 | Fujitsu Ltd | Information processor |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008136960A (en) * | 2006-12-04 | 2008-06-19 | Fuji Electric Holdings Co Ltd | Activated sludge treatment apparatus and activated sludge treatment method |
| JP2017006844A (en) * | 2015-06-19 | 2017-01-12 | 株式会社神鋼環境ソリューション | Digestion treatment device and digestion treatment method |
-
1984
- 1984-03-13 JP JP59046568A patent/JPS60190297A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04148445A (en) * | 1990-10-12 | 1992-05-21 | Fujitsu Ltd | Information processor |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60190297A (en) | 1985-09-27 |
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