JPH09253684A - Treatment method for organic waste water - Google Patents
Treatment method for organic waste waterInfo
- Publication number
- JPH09253684A JPH09253684A JP6823696A JP6823696A JPH09253684A JP H09253684 A JPH09253684 A JP H09253684A JP 6823696 A JP6823696 A JP 6823696A JP 6823696 A JP6823696 A JP 6823696A JP H09253684 A JPH09253684 A JP H09253684A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- activated sludge
- treatment system
- amount
- activated
- 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
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は下水などの有機性汚
水を生物処理する場合に実質的に余剰汚泥の発生量をゼ
ロにできる新規な生物処理技術に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a novel biological treatment technique capable of substantially reducing the amount of excess sludge generated when biologically treating organic sewage such as sewage.
【０００２】[0002]
【従来の技術】下水などの有機性汚水の活性汚泥法など
の生物処理工程から大量の汚泥（生汚泥、余剰汚泥）が
発生しており、汚泥の処理処分が現在最大の問題になっ
ている。従来これらの汚泥は脱水助剤（ポリマなど）を
添加し脱水機で脱水されたのち焼却処分されているが、
汚泥が大量な場合、脱水助剤添加費、脱水機、焼却炉規
模が大規模なものになり、ユーザーにとって大きな負担
になっている。また汚泥焼却灰の発生量も多く焼却灰の
処分にも苦慮している。2. Description of the Related Art A large amount of sludge (raw sludge, surplus sludge) is generated from a biological treatment process such as an activated sludge method of organic wastewater such as sewage, and sludge treatment and disposal is currently the biggest problem. . Conventionally, these sludges have been dehydrated with a dehydrating aid (polymer etc.) and then incinerated.
When a large amount of sludge is added, the cost of adding a dehydration aid, the dehydrator, and the scale of the incinerator become large, which imposes a heavy burden on users. In addition, the amount of sludge incinerated ash is large and it is difficult to dispose of the incinerated ash.
【０００３】従来より余剰汚泥の減量化法として嫌気性
消化（メタン発酵）法があるが、長い滞留日数を必要と
する割りには減量化効果が劣り、汚泥発生量をゼロにす
ることはできず、嫌気性消化後に残留する消化汚泥を結
局、脱水・焼却処分しなければならなかった。また余剰
生物汚泥をオゾン酸化して可溶化した後、好気性生物処
理槽に供給し汚泥を減量化する方法（特開平７−１１６
６８５）も知られているが、オゾン酸化槽での発泡トラ
ブル、排オゾン処理の必要性、オゾン添加コストが高
額、オゾン発生機の設備の高さなどの問題があり実用性
が乏しい。Conventionally, there is an anaerobic digestion (methane fermentation) method as a method for reducing excess sludge, but the reduction effect is inferior in comparison with the long retention days required, and the amount of sludge generated cannot be reduced to zero. First, the digested sludge remaining after anaerobic digestion had to be dehydrated and incinerated. In addition, a method of oxidizing excess biological sludge by ozone oxidation to solubilize it and then supplying it to an aerobic biological treatment tank to reduce the amount of sludge (Japanese Patent Laid-Open No. 7-116
685) is also known, but its practicality is poor due to problems such as foaming troubles in the ozone oxidation tank, necessity of exhaust ozone treatment, high cost of ozone addition, and high equipment of ozone generator.
【０００４】[0004]
【発明が解決しようとする課題】本発明は下水、屎尿、
食品工場廃水などの有機性汚水の生物処理施設から発生
する余剰汚泥を効果的に減容化し、実質的に余剰汚泥が
発生しなくなる新技術を提供することを課題にする。The present invention is directed to sewage, human waste,
It is an object of the present invention to effectively reduce the volume of surplus sludge generated from a biological treatment facility for organic wastewater such as food factory wastewater and to provide a new technology in which the surplus sludge is substantially not generated.
【０００５】[0005]
【課題を解決するための手段】本発明は汚泥の嫌気性発
酵法を新規な態様で汚水の好気性生物処理系と結合し、
余剰汚泥を効果的に減容化する新技術を見出して完成さ
れたものである。本発明は、有機性汚水を活性汚泥処理
系にて処理する方法において、該活性汚泥処理系の活性
汚泥増殖量より多い汚泥量を活性汚泥処理系から引き抜
き、この引き抜き汚泥を嫌気性発酵工程にて発酵処理せ
しめた後、活性汚泥処理系に返送して好気性生物処理す
ることを特徴とする有機性汚水の処理方法である。The present invention combines an anaerobic fermentation process for sludge with a novel aerobic biological treatment system for wastewater,
It was completed by finding a new technology to effectively reduce excess sludge volume. The present invention is a method of treating organic wastewater with an activated sludge treatment system, in which a sludge amount larger than the activated sludge growth amount of the activated sludge treatment system is drawn from the activated sludge treatment system, and the drawn sludge is subjected to an anaerobic fermentation step. It is a method for treating organic sewage, which comprises fermenting the sewage by fermentation and returning it to an activated sludge treatment system for aerobic biological treatment.
【０００６】本発明にいう「活性汚泥処理系」とは有機
性汚水を活性汚泥の存在下に生物処理する系であり、活
性汚泥法、生物学的硝化脱窒素法、嫌気好気活性汚泥
法、生物膜法、流動担体添加法などを含む意味で用いて
おり、プロセス全体の中に少なくとも活性汚泥による好
気的な生物処理工程を含む生物処理法の意味で用いてい
る。The "activated sludge treatment system" referred to in the present invention is a system for biologically treating organic wastewater in the presence of activated sludge, and includes activated sludge method, biological nitrification denitrification method, anaerobic aerobic activated sludge method. , Biofilm method, fluidized carrier addition method, etc., and used in the sense of a biological treatment method that includes at least an aerobic biological treatment step with activated sludge in the whole process.
【０００７】また、本発明において、嫌気性発酵工程に
おける発酵処理は従来公知の方法、装置が適用される。Further, in the present invention, conventionally known methods and apparatuses are applied to the fermentation treatment in the anaerobic fermentation process.
【０００８】[0008]
【発明の実施の形態】以下、図１を参照して本発明の作
用原理を説明する。有機性汚水１は活性汚泥処理系２に
導入されて処理される。活性汚泥処理系２から活性汚泥
増殖量以上の汚泥を固液分離工程３もしくは直接に引き
抜き汚泥４として引き抜くと共に処理水５を得る。引き
抜き汚泥４は嫌気性発酵工程６にて発酵処理され、この
発酵処理された汚泥７は活性汚泥処理系２に返送され
る。この結果、嫌気性発酵汚泥中の有機物が好気性生物
により生物分解されて除去され、これにより系全体から
排出される汚泥量が減少する。DETAILED DESCRIPTION OF THE INVENTION The principle of operation of the present invention will be described below with reference to FIG. The organic sewage 1 is introduced into the activated sludge treatment system 2 and treated. From the activated sludge treatment system 2, sludge having an activated sludge growth amount or more is drawn out as a sludge 4 in the solid-liquid separation step 3 or directly, and treated water 5 is obtained. The drawn sludge 4 is fermented in the anaerobic fermentation step 6, and the fermented sludge 7 is returned to the activated sludge treatment system 2. As a result, the organic matter in the anaerobic fermented sludge is biodegraded and removed by the aerobic organism, thereby reducing the amount of sludge discharged from the entire system.
【０００９】活性汚泥処理系２から引き抜き汚泥４を引
き抜く場合の固液分離工程３としては、沈降分離、凝集
分離、遠心分離、膜分離等の公知の処理が適用できる。
引き抜き汚泥の嫌気性発酵工程６としては、酸発酵もし
くはメタン発酵を適用することができる。酸発酵を適用
する場合は、汚泥は酸生成菌の酵素によって加水分解さ
れて３０〜４０％程度可溶化し可溶性の有機酸（例え
ば、酢酸、プロピオン酸、酪酸など）が生成する。この
発酵処理された汚泥７は、活性汚泥処理系２に返送さ
れ、有機酸の全てと可溶化しなかった嫌気性汚泥の一部
が好気性生物により分解、除去される。Known processes such as sedimentation separation, coagulation separation, centrifugal separation, and membrane separation can be applied as the solid-liquid separation step 3 in the case of extracting the sludge 4 drawn from the activated sludge treatment system 2.
As the anaerobic fermentation step 6 of the drawn sludge, acid fermentation or methane fermentation can be applied. When acid fermentation is applied, the sludge is hydrolyzed by an enzyme of an acid-producing bacterium to be solubilized by about 30 to 40% and a soluble organic acid (for example, acetic acid, propionic acid, butyric acid, etc.) is generated. The fermentation-treated sludge 7 is returned to the activated sludge treatment system 2, and all of the organic acids and part of the anaerobic sludge that has not been solubilized are decomposed and removed by the aerobic organism.
【００１０】メタン発酵を適用する場合は、有機酸は嫌
気性発酵過程でメタンガスに転換され分解するので、活
性汚泥処理系２には有機酸は流入せず、嫌気性発酵工程
で可溶化しなかった嫌気性汚泥が該処理系２の好気性微
生物により資化され、その一部が分解される。尚、嫌気
性発酵工程６から流出する発酵処理された汚泥７を膜、
遠心分離などの手段により固液分離し、汚泥の嫌気性発
酵工程のＳＲＴ（固形物滞留時間）を長くすると可溶化
率を更に向上できる。When methane fermentation is applied, the organic acid is converted to methane gas in the anaerobic fermentation process and decomposes, so that the organic acid does not flow into the activated sludge treatment system 2 and is not solubilized in the anaerobic fermentation process. The anaerobic sludge is assimilated by the aerobic microorganisms of the treatment system 2, and a part of it is decomposed. The fermentation sludge 7 flowing out from the anaerobic fermentation step 6 is formed into a film,
The solubilization rate can be further improved by solid-liquid separation by means such as centrifugation and increasing the SRT (solids retention time) in the sludge anaerobic fermentation process.
【００１１】酸発酵を適用する場合、嫌気性発酵工程の
滞留時間はメタン発酵を適用する場合よりも少なくて済
む利点があるが、生成した有機酸を活性汚泥処理系の好
気性生物処理で分解しなければならないので酸素消費量
が増加し曝気ブロワ動力が増加する欠点がある。従っ
て、設備建設費を重視する場合は、嫌気性発酵工程で使
用する槽が小さくてすむ酸発酵を適用し、消費エネルギ
ーの削減を重視する場合は、メタン発酵法を採用するの
がよい。When acid fermentation is applied, the residence time of the anaerobic fermentation process is shorter than when methane fermentation is applied, but the organic acid produced is decomposed by aerobic biological treatment in an activated sludge treatment system. Therefore, there is a disadvantage that oxygen consumption increases and aeration blower power increases. Therefore, when the equipment construction cost is emphasized, it is preferable to apply the acid fermentation in which the tank used in the anaerobic fermentation process can be small, and when the reduction of energy consumption is emphasized, the methane fermentation method is preferably adopted.
【００１２】酸発酵の滞留時間は３〜５日、メタン発酵
の滞留時間は７〜１０日程度に設定する。嫌気性発酵工
程の温度は、酸発酵法の場合は常温〜８０℃程度、メタ
ン発酵の場合は２５〜３５℃の中温程度、もしくは５５
〜６０℃の高温消化領域に設定する。The residence time of acid fermentation is set to 3 to 5 days, and the residence time of methane fermentation is set to about 7 to 10 days. The temperature of the anaerobic fermentation step is from room temperature to about 80 ° C. in the case of the acid fermentation method, 25 to 35 ° C. in the case of methane fermentation, or 55.
Set in the high temperature digestion region of -60 ° C.
【００１３】酸発酵の温度は無加温よりも加温したほう
が可溶化率が向上するほか、嫌気性発酵後の汚泥を曝気
槽に供給した場合の汚泥の生物分解性が向上するので好
ましい。加温熱量を削減するために引き抜き汚泥４は、
生物汚泥をあらかじめ遠心分離などの手段によって濃縮
し液量を減少することが好ましい。It is preferable that the temperature of the acid fermentation is higher than that without heating because the solubilization rate is improved and the biodegradability of sludge when the sludge after anaerobic fermentation is supplied to the aeration tank is improved. In order to reduce the heating amount, the drawn sludge 4
It is preferable to concentrate the biological sludge in advance by means such as centrifugation to reduce the amount of liquid.
【００１４】引き抜き汚泥４を嫌気性発酵処理する量を
多くするほど、汚泥の減容率は高くなる。なお、嫌気性
発酵処理後の汚泥を好気性生物処理すると好気性汚泥が
増殖するので、単に活性汚泥処理系からの活性汚泥増殖
量（従来法における余剰汚泥相当量）を嫌気性発酵工程
で処理しただけでは本発明において余剰汚泥量をゼロに
することはできない。従って、活性汚泥処理系で増殖す
る汚泥量が見かけ上ゼロになるように活性汚泥処理系か
ら該増殖量より過剰の活性汚泥を引き抜いて嫌気性発酵
させることにより、系全体から生じる余剰汚泥量を実質
的にゼロにできる。The larger the amount of anaerobic fermentation treatment of the drawn sludge 4, the higher the sludge volume reduction rate. In addition, since aerobic sludge grows when aerobic biological treatment of sludge after anaerobic fermentation treatment, the amount of activated sludge growth from the activated sludge treatment system (equivalent amount of excess sludge in the conventional method) is treated in the anaerobic fermentation process. Only by doing so, the amount of excess sludge cannot be made zero in the present invention. Therefore, by extracting anaerobic fermentation by extracting excess activated sludge from the activated sludge treatment system so that the amount of sludge that proliferates in the activated sludge treatment system becomes apparently zero, the excess sludge amount generated from the entire system is reduced. Can be virtually zero.
【００１５】即ち、図２に示すような従来の活性汚泥法
において余剰汚泥１０として廃棄されていた部分（例え
ば、沈殿汚泥８から返送汚泥９を除いた残部）を引き抜
いて嫌気性発酵処理しても、活性汚泥は増加し、必然的
に余剰汚泥が発生するので従来、余剰汚泥といて破棄さ
れていた汚泥量以上を嫌気性発酵させる必要がある。こ
のことによって、はじめて余剰汚泥を実質的にゼロにで
きる。That is, a portion that has been discarded as an excess sludge 10 in the conventional activated sludge method as shown in FIG. 2 (for example, the remaining portion except the returned sludge 9 from the settled sludge 8) is extracted and subjected to an anaerobic fermentation treatment. However, since activated sludge increases and excess sludge is inevitably generated, it is necessary to anaerobically ferment more sludge than is conventionally discarded as excess sludge. Only then can the surplus sludge be substantially reduced to zero.
【００１６】例えば、嫌気性発酵工程の汚泥可溶化率が
３０％の場合、通常の活性汚泥法で発生する余剰汚泥量
の約３倍量を引き抜いて嫌気性発酵処理後に活性汚泥処
理系に返送すれば、余剰汚泥の発生量をゼロにできる。
尚、図１において引き抜き汚泥４の一部を返送汚泥とし
て活性汚泥処理系２に返送してもよい。For example, when the sludge solubilization rate in the anaerobic fermentation step is 30%, about 3 times the amount of surplus sludge generated by the usual activated sludge method is extracted and returned to the activated sludge treatment system after the anaerobic fermentation treatment. By doing so, the amount of excess sludge generated can be reduced to zero.
In addition, in FIG. 1, part of the drawn sludge 4 may be returned to the activated sludge treatment system 2 as return sludge.
【００１７】[0017]
実施例１ 下水を対象に図１の工程に従って本発明の試験を行っ
た。表１に下水水質を示す。嫌気性発酵工程として温度
７０℃に加温して酸発酵する方法を適用した。Example 1 The test of the present invention was conducted on sewage according to the process shown in FIG. Table 1 shows the sewage quality. As the anaerobic fermentation step, a method of heating to a temperature of 70 ° C. and performing acid fermentation was applied.
【００１８】[0018]
【表１】 [Table 1]
【００１９】試験条件を表２に示す。The test conditions are shown in Table 2.
【００２０】[0020]
【表２】 [Table 2]
【００２１】表２の条件で１年間の試験を行った結果、
酸発酵での汚泥可溶化率は３８〜４５％であり、図１の
システム系外に排出される余剰汚泥発生量は一月あたり
約０．３〜０．７ｇ・ＳＳと極めて少量であった。また
処理水質は表３のように良好であった。As a result of conducting a test for one year under the conditions shown in Table 2,
The sludge solubilization rate in acid fermentation was 38 to 45%, and the amount of excess sludge generated outside the system of FIG. 1 was an extremely small amount of about 0.3 to 0.7 g · SS per month. . The treated water quality was good as shown in Table 3.
【００２２】[0022]
【表３】 [Table 3]
【００２３】実施例２ 実施例１における嫌気性発酵槽にかえてメタン発酵槽を
設けて試験した。メタン発酵槽の滞留時間は１０日、水
温は３６℃に設定した。その他の条件は実施例１と同じ
である。メタン発酵槽の汚泥減少率は５０〜５５％であ
り、活性汚泥処理系からの余剰汚泥の発生量は１２カ月
の試験期間中ゼロであった。Example 2 A methane fermentation tank was provided in place of the anaerobic fermentation tank in Example 1 for testing. The residence time of the methane fermentation tank was set to 10 days, and the water temperature was set to 36 ° C. Other conditions are the same as in the first embodiment. The sludge reduction rate of the methane fermentation tank was 50 to 55%, and the amount of excess sludge generated from the activated sludge treatment system was zero during the 12-month test period.
【００２４】比較例１ 図１から嫌気性発酵槽を除去し、通常の活性汚泥法で比
較試験を行った結果、汚泥発生量は、余剰汚泥が約２０
ｇ／月と多量であった。これは本発明の実施例１の数十
倍に相当する。Comparative Example 1 As a result of removing the anaerobic fermenter from FIG. 1 and conducting a comparative test by the usual activated sludge method, the amount of sludge generated was about 20 for excess sludge.
It was a large amount of g / month. This corresponds to several tens of times of the first embodiment of the present invention.
【００２５】[0025]
１．通常の活性汚泥法で生成する余剰汚泥量以上の活性
汚泥を引き抜き、嫌気性発酵により汚泥を可溶化し活性
汚泥処理系に返送するようにしたので、余剰汚泥を効果
的に減容化でき、従来の汚泥脱水工程、汚泥焼却工程が
不要になるか、もしくは著しく小規模化できる。 ２．従って、汚泥焼却灰がほとんど発生しない。条件に
よっては焼却灰が発生しないので、汚泥処分が著しく合
理化できる。 ３．オゾンを用いる必要がないので運転コスト設備コス
トが安価である。1. Since the amount of activated sludge in excess of the amount of excess sludge produced by the ordinary activated sludge method was drawn out and the sludge was solubilized by anaerobic fermentation and returned to the activated sludge treatment system, the excess sludge can be effectively reduced in volume, The conventional sludge dewatering process and sludge incineration process are not required or can be significantly reduced in size. 2. Therefore, sludge incineration ash hardly occurs. Depending on the conditions, incineration ash is not generated, so sludge disposal can be significantly streamlined. 3. Since it is not necessary to use ozone, operating costs and equipment costs are low.
【００２６】またオゾン酸化工程の激しい発泡を解決で
きる。Further, severe foaming in the ozone oxidation step can be solved.
【図１】本発明の一例を説明するための図である。FIG. 1 is a diagram illustrating an example of the present invention.
【図２】従来法を説明するための図である。FIG. 2 is a diagram for explaining a conventional method.
１ 有機性汚水 ２ 活性汚泥処理系 ３ 固液分離工程 ４ 引き抜き汚泥 ５ 処理水 ６ 嫌気性発酵工程 ７ 発酵処理された汚泥 ８ 沈殿汚泥 ９ 返送汚泥 １０ 余剰汚泥 1 Organic Sewage 2 Activated Sludge Treatment System 3 Solid-Liquid Separation Process 4 Extracted Sludge 5 Treated Water 6 Anaerobic Fermentation Process 7 Fermented Sludge 8 Settled Sludge 9 Returned Sludge 10 Excess Sludge
Claims (2)
る方法において、該活性汚泥処理系の活性汚泥増殖量よ
り多い汚泥量を活性汚泥処理系から引き抜き、この引き
抜き汚泥を嫌気性発酵工程にて発酵処理せしめた後、活
性汚泥処理系に返送して好気性生物処理することを特徴
とする有機性汚水の処理方法。1. A method for treating organic wastewater with an activated sludge treatment system, wherein a sludge amount larger than the activated sludge growth amount of the activated sludge treatment system is withdrawn from the activated sludge treatment system, and the extracted sludge is subjected to an anaerobic fermentation step. The method for treating organic sewage is characterized in that after the fermentation treatment is carried out in step 1, it is returned to the activated sludge treatment system for aerobic biological treatment.
ロであることを特徴とする請求項１に記載の有機性汚水
の処理方法。2. The method for treating organic sewage according to claim 1, wherein the excess sludge discharged to the outside of the system is substantially zero.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6823696A JP3485220B2 (en) | 1996-03-25 | 1996-03-25 | Organic wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6823696A JP3485220B2 (en) | 1996-03-25 | 1996-03-25 | Organic wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09253684A true JPH09253684A (en) | 1997-09-30 |
| JP3485220B2 JP3485220B2 (en) | 2004-01-13 |
Family
ID=13367960
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6823696A Expired - Fee Related JP3485220B2 (en) | 1996-03-25 | 1996-03-25 | Organic wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3485220B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002316182A (en) * | 2001-04-23 | 2002-10-29 | Kurita Water Ind Ltd | Method for treating organic waste liquid |
| JP2005279551A (en) * | 2004-03-30 | 2005-10-13 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| JP2006043511A (en) * | 2004-07-30 | 2006-02-16 | Sumitomo Heavy Ind Ltd | Organic acid producing method, organic acid producing device and wastewater treatment apparatus |
| US7560027B2 (en) | 2002-07-03 | 2009-07-14 | Jfe Engineering Corporation | Method for treating wastewater and sludge |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786780B (en) * | 2010-02-22 | 2013-04-03 | 北京能效环境工程有限公司 | Activated sludge treatment method |
-
1996
- 1996-03-25 JP JP6823696A patent/JP3485220B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002316182A (en) * | 2001-04-23 | 2002-10-29 | Kurita Water Ind Ltd | Method for treating organic waste liquid |
| US7560027B2 (en) | 2002-07-03 | 2009-07-14 | Jfe Engineering Corporation | Method for treating wastewater and sludge |
| JP2005279551A (en) * | 2004-03-30 | 2005-10-13 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| JP4501496B2 (en) * | 2004-03-30 | 2010-07-14 | 栗田工業株式会社 | Biological treatment method for organic wastewater |
| JP2006043511A (en) * | 2004-07-30 | 2006-02-16 | Sumitomo Heavy Ind Ltd | Organic acid producing method, organic acid producing device and wastewater treatment apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3485220B2 (en) | 2004-01-13 |
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