JPH02227191A - Treatment of organic sewage - Google Patents
Treatment of organic sewageInfo
- Publication number
- JPH02227191A JPH02227191A JP1045393A JP4539389A JPH02227191A JP H02227191 A JPH02227191 A JP H02227191A JP 1045393 A JP1045393 A JP 1045393A JP 4539389 A JP4539389 A JP 4539389A JP H02227191 A JPH02227191 A JP H02227191A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- tank
- supplied
- biological treatment
- sedimentation
- 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
- 239000010865 sewage Substances 0.000 title claims abstract description 18
- 239000010802 sludge Substances 0.000 claims abstract description 102
- 238000000034 method Methods 0.000 claims abstract description 21
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 239000005416 organic matter Substances 0.000 claims description 2
- 238000005273 aeration Methods 0.000 abstract description 19
- 238000004062 sedimentation Methods 0.000 abstract description 9
- 239000003513 alkali Substances 0.000 abstract description 3
- 230000003381 solubilizing effect Effects 0.000 abstract 2
- 241000894006 Bacteria Species 0.000 abstract 1
- 230000007928 solubilization Effects 0.000 description 13
- 238000005063 solubilization Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000007787 solid Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000009193 crawling Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 238000005227 gel permeation chromatography Methods 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000010800 human waste Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 239000000126 substance Substances 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)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、有機性汚水の処理方法に係り％特に、下水、
し尿、各種産業排水などの有機性汚水の好気性生物処理
と発生する汚泥の処理方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for treating organic sewage, particularly sewage,
This paper relates to aerobic biological treatment of organic sewage such as human waste and various industrial wastewater, and a method of treating the generated sludge.
従来、有機性汚水の好気性生物処理（活性汚泥法、硝化
脱窒法など）の最大の問題点は、余剰汚泥発生量が多い
点にあり、これらの汚泥は脱水、乾燥、焼却 処分など
の汚泥処理によって処分されていたが、その処分には多
大の経費と設備費がかかる。従来の活性汚泥法の余剰汚
泥の発生量は、除去されたＢＯＤ当り、α６〜α８ｋｇ
ａａ／除去ＢＯＤであり、非常に多量の余剰汚泥が発生
することがよく知られている。しかも、余剰汚泥は質的
にも、難脱水性であるため、ますます汚泥処理が困難に
なっている。Conventionally, the biggest problem with aerobic biological treatment of organic wastewater (activated sludge method, nitrification-denitrification method, etc.) is that it generates a large amount of surplus sludge, and this sludge is treated as sludge from dewatering, drying, incineration, etc. It was previously disposed of through processing, but such disposal requires a large amount of expense and equipment costs. The amount of surplus sludge generated by the conventional activated sludge method is α6 to α8 kg per removed BOD.
aa/removed BOD, and it is well known that a very large amount of surplus sludge is generated. In addition, surplus sludge is qualitatively difficult to dewater, making sludge treatment increasingly difficult.
本発明は、前記のような従来技術の問題点を解消し、生
物処理に伴って発生する余剰汚泥の発生量を著しく減少
させることが可能な新規な方法を提供することを目的と
する。An object of the present invention is to provide a novel method capable of solving the problems of the prior art as described above and significantly reducing the amount of surplus sludge generated due to biological treatment.
上記目的を達成するために、本発明では、有機性汚水を
、好気性生物処理したのち、固液分離し、該固液分離さ
れた汚泥の一部を、前記生物処理槽に返送する一方、汚
泥の他部にアルカリ剤を添加し、常温又は加温条件下で
滞留せしめて、汚泥中の有機物を可溶化せしめたのち、
前記生物処理槽に供給することｔ−特徴とする有機性汚
水の処理方法としたものである。In order to achieve the above object, in the present invention, organic wastewater is subjected to aerobic biological treatment, then subjected to solid-liquid separation, and a part of the solid-liquid separated sludge is returned to the biological treatment tank, while After adding an alkaline agent to the other part of the sludge and allowing it to remain at room temperature or under heated conditions to solubilize the organic matter in the sludge,
A method for treating organic wastewater characterized by supplying it to the biological treatment tank.
次に、本発明を第１図を参照にして詳しく説明する。以
下は下水処理を例に挙げて説明している。Next, the present invention will be explained in detail with reference to FIG. The following explanation uses sewage treatment as an example.
ｉ＠１図は、本発明の有機性汚水の処理方法を示す工程
図である。流入下水１は、曝気槽２に流入し、ＢＯＤ資
化活性汚泥の共存下で所定時間曝気され°たのち、沈殿
槽５に流入し、活性汚泥が沈降され、清澄な処理水４と
なる。５は散水装置である。Figure i@1 is a process diagram showing the method for treating organic wastewater of the present invention. The inflowing sewage 1 flows into the aeration tank 2 and is aerated for a predetermined time in the coexistence of BOD assimilation activated sludge, and then flows into the settling tank 5 where the activated sludge settles and becomes clear treated water 4. 5 is a water sprinkler device.
沈殿槽のかわりに公知の固液分離手段、例えば遠心分離
、浮上分離、ＵＰ膜又はＭＰ膜の膜分離でもかまわない
。また、沈降分離汚泥を、さらに遠心分離機等で濃縮し
て、次の処理工程に供給することができる。In place of the sedimentation tank, known solid-liquid separation means such as centrifugation, flotation, UP membrane or MP membrane separation may be used. In addition, the settled sludge can be further concentrated using a centrifuge or the like and then supplied to the next treatment step.
沈降分離汚泥６０大部分は、返送汚泥管７から曝気槽２
にリサイクルされ、曝気槽２内のＭＬ８Ｂを所定濃度に
維持する。一方、沈降分離汚泥６の他部８は、汚泥濃縮
工程９（遠心分離機が、汚泥濃縮度を最も高くできるの
で最適である）に供給され、固形物濃度５〜８％程度に
濃縮されたのち、濃縮汚泥１０の一部が汚泥脱水工程１
５に導かれ、他部が汚泥可溶化槽１１（汚泥の加水分解
槽と呼ぶこともある）に供給される。そしてＮａＯＨ％
Ｃａ（ＯＨ）１などのアルカリ剤１２を汚泥可溶化槽１
１に添加し、 ｐＨＩ ０以上（好ましく ｑ ｐＨ１
２以上）として、所要時間（通常１〜２４ｈｒで、所要
時間は汚泥の質によって変化する）滞留させる。汚泥の
可溶化槽１１の温度は、可溶化（加水分解）速度を速め
るため、加温（５０〜１００℃が好適）するのが好まし
い。また、ここで超音波を作用させるとより効果的に可
溶化できる。Most of the settled and separated sludge 60 is transferred from the return sludge pipe 7 to the aeration tank 2.
The ML8B in the aeration tank 2 is maintained at a predetermined concentration. On the other hand, the other part 8 of the sedimentation and separation sludge 6 is supplied to a sludge concentration step 9 (a centrifugal separator is optimal because it can achieve the highest sludge concentration), and is concentrated to a solids concentration of about 5 to 8%. Later, a part of the thickened sludge 10 is transferred to the sludge dewatering process 1.
5, and the other part is supplied to a sludge solubilization tank 11 (sometimes called a sludge hydrolysis tank). and NaOH%
Add an alkaline agent 12 such as Ca(OH)1 to the sludge solubilization tank 1.
1, pHI 0 or more (preferably q pH1
2 or more) for the required time (usually 1 to 24 hours, the required time varies depending on the quality of the sludge). The temperature of the sludge solubilization tank 11 is preferably heated (50 to 100° C. is preferable) in order to accelerate the solubilization (hydrolysis) rate. Further, if ultrasonic waves are applied here, solubilization can be more effectively achieved.
可溶化槽１１においては、活性汚泥を構成する徨々の微
生物の細胞構成成分（ポリサッカライド、プロティンな
ど）が、アルカリ条件下で加水分解されて低分子化され
、分子量数千〜数万の分子コロイド領域状態にまで可溶
化されることが、ゲルクロマトグラフィーによる分析に
よって見出された。可溶化された汚泥は高ＩＩＩ度のＢ
ＯＤ成分を含むことも認められた。また、汚泥の一部（
数嘩）は可溶化されずに、８８状のままで残る現象も認
められた。１７は加熱器であり、ｔｓＦｉ濃縮工程分離
水である。In the solubilization tank 11, the cellular components of the various microorganisms that make up the activated sludge (polysaccharides, proteins, etc.) are hydrolyzed under alkaline conditions and reduced in molecular weight to molecules with a molecular weight of several thousand to tens of thousands. It was found by gel chromatography analysis that it was solubilized to a colloidal state. The solubilized sludge has a high degree of B
It was also recognized that it contained an OD component. In addition, some of the sludge (
A phenomenon was also observed in which the 88-shaped particles remained as they were without being solubilized. 17 is a heater, which is tsFi concentration process separated water.
なお、沈降汚泥６の固形物濃度が高い場合は、汚泥濃縮
工程９を設ける必要はない。この工程は絶対必要条件で
はなく、沈降汚泥６をそのまま、汚泥脱水工程１５およ
び汚泥可溶化槽１１に供給しても構わないが、大部分の
ケースには汚泥濃縮工程９を介在させるほうが、はるか
に好ましい。なぜなら、汚泥可溶化槽１１に供給するＮ
ａＯＨなどの公知のアルカリ剤の所要量が、汚泥ａｍ度
に反比例して増加するので、可能な限り、固形物濃度の
高い汚泥を可溶化槽１１に供給することが、望ましいか
らである。Note that if the solid matter concentration of the settled sludge 6 is high, it is not necessary to provide the sludge concentration step 9. This step is not an absolute requirement, and the settled sludge 6 may be supplied as is to the sludge dewatering step 15 and the sludge solubilization tank 11, but in most cases it is much better to include the sludge concentration step 9. preferred. This is because N supplied to the sludge solubilization tank 11
This is because the required amount of a known alkaline agent such as aOH increases in inverse proportion to the am content of the sludge, so it is desirable to supply sludge with a high solids concentration to the solubilization tank 11 as much as possible.
アルカリにより加水分解された低分子性のＢＯＤを含む
可溶化汚泥１４は、曝気槽２あるいは汚泥返送ライン７
に供給され、曝気槽２内に存在する活性汚泥によって、
ＣＯ，とＨ，Ｏに生物学的に分解される。もちろん、
曝気槽２へのＢＯＤ負荷は、流入下水のＢＯＤと可溶化
汚泥のＢＯＤの合計量に基づいて、設計し、処理水質の
悪化をあらかじめ防止するようにしておくことが重要で
ある。The solubilized sludge 14 containing low-molecular BOD hydrolyzed by alkali is transported to the aeration tank 2 or the sludge return line 7.
The activated sludge supplied to the aeration tank 2 and present in the aeration tank 2
Biologically decomposed into CO, H, and O. of course,
It is important to design the BOD load to the aeration tank 2 based on the total amount of BOD of inflowing sewage and BOD of solubilized sludge to prevent deterioration of treated water quality in advance.
なお、既設の活性汚泥プロセスに本発明を適用しようと
する場合は、既設の曝気槽２の容量を増加することは固
離な場合が多いので、曝気槽のＭＬ８Ｂ濃度を高めるこ
とによって対応し次はうが好ましい。Note that when applying the present invention to an existing activated sludge process, increasing the capacity of the existing aeration tank 2 often results in solidification, so the next step is to increase the ML8B concentration in the aeration tank. Crawling is preferred.
以上が不発明の処理工程であり、本発明者の６ケ月間に
渡るロングランテストにより、余剰汚泥の発生量が、従
来の活性汚泥法に比較して、曇〜Ａに減少することが確
認された。ま九、下水などには粘土分などの無機性の８
Ｓなども含まれているので、余剰汚泥発生量がゼロにな
ることは、あり得ないので、余剰汚泥排出管１０′を設
け、汚泥脱水機１５によって、脱水するようにしておく
べきである。１６は汚泥脱水ケーキである。The above is an uninvented treatment process, and the inventor's long run test over 6 months confirmed that the amount of surplus sludge generated was reduced to cloudy to A compared to the conventional activated sludge method. Ta. Inorganic substances such as clay are present in sewage, etc.
Since S and the like are included, it is impossible for the amount of surplus sludge generated to be zero. Therefore, a surplus sludge discharge pipe 10' should be provided and the sludge should be dewatered by a sludge dewatering machine 15. 16 is a sludge dewatering cake.
以下、実施例により本発明をより詳しく説明するが、本
発明はこれらの実施例に限定されない。EXAMPLES Hereinafter, the present invention will be explained in more detail with reference to Examples, but the present invention is not limited to these Examples.
実施例１ 初沈越流下水（ＢＯＤ １２０５１８０９／ｌ。Example 1 First settling overflow sewage (BOD 12051809/l.
８８ １００〜１５５１９／ｊ ） ｔ−曝気時間８
ｈｒ。88 100-15519/j) t-Aeration time 8
hr.
活性汚泥ＭＬ８８１８００〜２５００ダ／ｌの曝気槽（
ＢＯＤ−ＭＬ８Ｂ負荷（Ｌ １８〜ｃＬ２５ （ｋｇＢ
ＯＤ／ＪＭＬ８８・日）に供給したのち、水面積負荷１
２ｍ１／ｍ”・日 の沈殿槽において、活性汚泥を沈降
分離し、固形物濃度１〜１．５１４の沈殿汚泥を得た。Activated sludge ML881800-2500 da/l aeration tank (
BOD-ML8B load (L 18~cL25 (kgB
OD/JML88・day), water area load 1
The activated sludge was separated by sedimentation in a settling tank of 2 m1/m''·day to obtain settled sludge with a solids concentration of 1 to 1.514.
下水処理量をＱ ｍ”１日とするとき、沈殿汚泥のαＯ
Ｉ Ｑ ｍ”７日を遠心分離機による汚泥１１＃１工程
に供給し、残りの沈殿汚泥は曝気槽に返送した。When the amount of sewage treatment is Q m” per day, αO of the settled sludge
I Q m''7 days was supplied to the sludge 11#1 process using a centrifuge, and the remaining settled sludge was returned to the aeration tank.
遠心濃縮機（巴工業製、シャープレス ＢＤ型スーパデ
カンタ−）により、沈殿汚泥を濃縮を得た。The precipitated sludge was concentrated using a centrifugal concentrator (Sharpless BD type super decanter manufactured by Tomoe Kogyo).
次にこの濃縮汚泥を、滞留時間１５時間の回分処理タイ
プの汚泥可溶化槽に導きスチームを吹きこんで、温度７
０〜７５℃に加温しつつ、ＮａＯＨを汚泥可溶化槽内液
に対し、α０５Ｎ〜（Ｌ２Ｎ１１度（ｐＨ１１〜１３）
になるように添加して、攪拌しながら汚泥の可溶化（７
７０水分解）を行った。しかるのち、可溶化汚泥（ｓｓ
ｓｏｏ。Next, this thickened sludge was introduced into a batch treatment type sludge solubilization tank with a residence time of 15 hours, and steam was blown into the tank to maintain a temperature of 7.
While heating to 0-75℃, add NaOH to the liquid in the sludge solubilization tank at α05N~(L2N11 degrees (pH 11-13)
Solubilize the sludge (7
70 water decomposition). After that, solubilized sludge (ss
Sooo.
〜７０ＱＱＩｎ９／ｌ、ＢＯＤ ８０００〜１１００
０Ｉｎ９／ｌ）を、前記の曝気槽に添加して、好気性、
生物処理を行った。~70QQIn9/l, BOD 8000~1100
0In9/l) was added to the aeration tank to create an aerobic
Biological treatment was performed.
６ケ月、上記の条件に従って運転を続けた結果、沈殿池
流出水の水質はＢＯＤ１８〜２５．８８２６〜５２ダ／
ｌであった。ま九、余剰汚泥、発生量の６ケ月間の変動
範囲は下水処理量１−ｍあたり、α０２７〜１１０３６
に９ｓ＋８であつ九。As a result of continuing operation according to the above conditions for 6 months, the water quality of the sedimentation tank effluent was BOD 18-25.8826-52 Da/
It was l. The fluctuation range of excess sludge and generated amount over a 6-month period is α027 to 11036 per 1 m of sewage treatment volume.
Atatsu nine with 9s+8.
また沈殿槽に流入する活性汚泥の８ＶＩ値は１５０〜２
００であった。In addition, the 8VI value of activated sludge flowing into the settling tank is 150 to 2.
It was 00.
比較例
第１図の本発明フローの、汚泥可溶化槽、Ｎａ０Ｉ（（
１）添加を省略し比以外は、同一条件（下水処理量、流
入下水水質、曝気槽滞留時間、ＢＯＤ −８Ｓ負荷を同
一にした）のテストを同一期間並行して行った結果、沈
殿槽に流入する活性汚泥スラリーの８ＶＩは１８０〜２
７０、沈殿流出水のＢＯＤ１２〜２０．８８２８〜３５
’１９／ｌであり、余剰汚泥発生量は下水処理１１ｍ’
あたりα１１〜（Ｌ １４ ｋｌｉｓｇであった。この
値は本発明に比べ約３〜４倍も多量であり、本発明効果
が大きいことが確認され九。Comparative Example The sludge solubilization tank, Na0I ((
1) As a result of conducting tests in parallel for the same period under the same conditions (sewage treatment amount, inflow sewage water quality, aeration tank residence time, and BOD-8S load were the same) except for the ratio, the addition was omitted. 8VI of the inflowing activated sludge slurry is 180-2
70, BOD of precipitation effluent 12-20.8828-35
'19/l, and the amount of surplus sludge generated is 11 m2 of sewage treatment.'
This value was about 3 to 4 times larger than that of the present invention, confirming that the effect of the present invention is large.
本発明によれば、次のような効果が得られる。 According to the present invention, the following effects can be obtained.
■ 簡単な操作、設備により、余剰汚泥の発生量を大幅
に減少できる。また汚泥の脱水、乾燥、焼却処分または
埋立処分が大幅に合理化でき、汚泥処理、処分工程の設
備費、経費も数分の１に節減できる。■ Easy operation and equipment can significantly reduce the amount of surplus sludge generated. In addition, the dewatering, drying, incineration, or landfill disposal of sludge can be greatly streamlined, and the equipment costs and expenses for sludge treatment and disposal processes can be reduced to a fraction of the cost.
■ 沈殿槽に流入する活性汚泥の沈降性が、やや向上す
る。■ The settling ability of activated sludge flowing into the settling tank is slightly improved.
第１図は、本発明の処理方法を示す工程図である。
１・・・流入下水、２・・・曝気槽、３・・・沈殿槽、
４・・・清澄な処理水、５・・・散気装置、６・・・沈
降分離汚泥、７・・・返送汚泥、８・・・処理用汚泥、
９・・・汚泥濃縮工程、１０・・・濃縮汚泥、１１・・
・汚泥可溶化槽、１２・・・アルカリ剤、１３・・・濃
縮工程分離水％ １４・・・可溶化汚泥
特許出願人 荏原インフィルコ株式会社同 株式会
社荏原総合研究所FIG. 1 is a process diagram showing the treatment method of the present invention. 1... Inflow sewage, 2... Aeration tank, 3... Sedimentation tank,
4...Clear treated water, 5...Aeration device, 6...Sedimentation and separation sludge, 7...Return sludge, 8...Sludge for treatment,
9...Sludge concentration process, 10...Thickened sludge, 11...
・Sludge solubilization tank, 12... Alkaline agent, 13... Separated water % in concentration process 14... Solubilized sludge patent applicant Ebara Infilco Co., Ltd. Ebara Research Institute, Inc.
Claims (1)
、該固液分離された汚泥の一部を前記生物処理槽に返送
する一方、汚泥の他部にアルカリ剤を添加し、常温もし
くは加温条件下で滞留せしめて、汚泥中の有機物を可溶
化せしめたのち、前記生物処理槽に供給することを特徴
とする有機性汚水の処理方法。1. After aerobic biological treatment of organic sewage, solid-liquid separation is carried out, and a part of the solid-liquid separated sludge is returned to the biological treatment tank, while an alkaline agent is added to the other part of the sludge, and the sludge is kept at room temperature. Alternatively, a method for treating organic sewage, which comprises retaining the sludge under heated conditions to solubilize organic matter in the sludge, and then supplying the sludge to the biological treatment tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4539389A JPH0661550B2 (en) | 1989-02-28 | 1989-02-28 | Organic wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4539389A JPH0661550B2 (en) | 1989-02-28 | 1989-02-28 | Organic wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02227191A true JPH02227191A (en) | 1990-09-10 |
| JPH0661550B2 JPH0661550B2 (en) | 1994-08-17 |
Family
ID=12718021
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4539389A Expired - Fee Related JPH0661550B2 (en) | 1989-02-28 | 1989-02-28 | Organic wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0661550B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6127167A (en) * | 1993-12-28 | 2000-10-03 | Honda Giken Kogyo Kabushiki Kaisha | Method of controlling proliferation of aerobe |
| WO2002088033A1 (en) * | 2000-10-06 | 2002-11-07 | Able Co., Ltd. | Method and device for reducing volume of excess sludge |
| WO2003097540A1 (en) * | 2002-05-22 | 2003-11-27 | Ebara Corporation | Method of treating organic waste water capable of phosphorus recovery and apparatus |
| JP2006346622A (en) * | 2005-06-17 | 2006-12-28 | Jfe Engineering Kk | Apparatus for treating excrement waste water |
| CN102701526A (en) * | 2012-05-31 | 2012-10-03 | 上海环保（集团）有限公司 | Treatment process and system of nutrient self compensation and difficult-to-degrade industrial wastewater |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5981096B2 (en) * | 2010-06-02 | 2016-08-31 | 日立造船株式会社 | Wastewater treatment method and apparatus |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3622507A (en) * | 1969-07-23 | 1971-11-23 | Tno | Activated sludge processing |
| JPS4911813A (en) * | 1972-04-12 | 1974-02-01 |
-
1989
- 1989-02-28 JP JP4539389A patent/JPH0661550B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3622507A (en) * | 1969-07-23 | 1971-11-23 | Tno | Activated sludge processing |
| JPS4911813A (en) * | 1972-04-12 | 1974-02-01 |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6127167A (en) * | 1993-12-28 | 2000-10-03 | Honda Giken Kogyo Kabushiki Kaisha | Method of controlling proliferation of aerobe |
| WO2002088033A1 (en) * | 2000-10-06 | 2002-11-07 | Able Co., Ltd. | Method and device for reducing volume of excess sludge |
| US6773597B2 (en) | 2000-10-06 | 2004-08-10 | Able Co., Ltd. | Method and apparatus for reducing excess sludge |
| WO2003097540A1 (en) * | 2002-05-22 | 2003-11-27 | Ebara Corporation | Method of treating organic waste water capable of phosphorus recovery and apparatus |
| JP2006346622A (en) * | 2005-06-17 | 2006-12-28 | Jfe Engineering Kk | Apparatus for treating excrement waste water |
| JP4506574B2 (en) * | 2005-06-17 | 2010-07-21 | Ｊｆｅエンジニアリング株式会社 | Human wastewater treatment equipment |
| CN102701526A (en) * | 2012-05-31 | 2012-10-03 | 上海环保（集团）有限公司 | Treatment process and system of nutrient self compensation and difficult-to-degrade industrial wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0661550B2 (en) | 1994-08-17 |
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|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |