JPH0724499A - Treatment of sludge - Google Patents
Treatment of sludgeInfo
- Publication number
- JPH0724499A JPH0724499A JP5196755A JP19675593A JPH0724499A JP H0724499 A JPH0724499 A JP H0724499A JP 5196755 A JP5196755 A JP 5196755A JP 19675593 A JP19675593 A JP 19675593A JP H0724499 A JPH0724499 A JP H0724499A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- treatment
- toc
- excess
- anaerobic
- 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
- 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]
【産業上の利用分野】本発明は有機性汚泥の処理方法に
関し、更に詳しくは排水を活性汚泥方式で処理して発生
する汚泥の余剰部分或は余剰汚泥の嫌気性硝化で発生す
る嫌気性硝化汚泥等の有機性汚泥を処理して、該汚泥を
減量化する有機性汚泥の処理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating organic sludge, and more specifically, an excess portion of sludge generated by treating wastewater with an activated sludge system or anaerobic nitrification caused by anaerobic nitrification of excess sludge. The present invention relates to a method for treating organic sludge such as sludge to reduce the amount of the sludge.
【０００２】[0002]
【従来の技術】従来、ＢＯＤで示される排水中の有機汚
濁成分の除去においては、現在実用化されている活性汚
泥方式等の生物学的処理方法によって、比較的低いコス
トで満足し得る結果が得られている。上記活性汚泥方式
では、図１に示す様に、処理対象排水を最初沈澱池に導
き、比重の重いものを沈澱させ、次いで曝気槽におい
て、活性汚泥によって排水中の有機物を分解させる。こ
の活性汚泥処理では、分解したＢＯＤのうちの５０〜７
０重量％は微生物の生活エネルギーに消費され、残りの
３０〜７０重量％は菌体の増殖に使用される為、余剰汚
泥が発生することになる。2. Description of the Related Art Conventionally, in the removal of organic pollutants in wastewater indicated by BOD, a biological treatment method such as an activated sludge system which has been put into practical use has been satisfactory at a relatively low cost. Has been obtained. In the activated sludge system, as shown in FIG. 1, the wastewater to be treated is first introduced into a settling tank to precipitate the one having a large specific gravity, and then the organic matter in the wastewater is decomposed by the activated sludge in the aeration tank. In this activated sludge treatment, 50 to 7 out of the decomposed BOD
Since 0% by weight is consumed for living energy of microorganisms and the remaining 30 to 70% by weight is used for the growth of bacterial cells, excess sludge is generated.
【０００３】活性汚泥処理で発生した余剰汚泥は、生物
難分解性であり且つ粘性が高いので、活性汚泥処理方式
では発生する余剰汚泥の処理が大きな問題となる。現
在、余剰汚泥の処理方法は、図２に示す様に、嫌気性硝
化により、余剰汚泥をメタンガス、二酸化炭素、水素、
硫化水素等に分解して減量化し、その後分解されなかっ
た余剰汚泥及びその他の固形物は脱水機等により分離さ
れ、焼却されるか或は産業廃棄物として処分される。
又、場合によっては余剰汚泥は嫌気性処理を行わずに直
接脱水機等により分離され、同様に焼却されるか或は産
業廃棄物として処分される。Excess sludge generated by the activated sludge treatment is biodegradable and has a high viscosity, so that the treatment of the excess sludge generated in the activated sludge treatment system is a serious problem. At present, as shown in FIG. 2, the method for treating excess sludge is to remove excess sludge from methane gas, carbon dioxide, hydrogen, by anaerobic nitrification.
Excess sludge and other solids that are not decomposed after being decomposed into hydrogen sulfide and the like to reduce the amount are separated by a dehydrator or the like and incinerated or disposed as industrial waste.
In some cases, excess sludge is directly separated by a dehydrator or the like without performing anaerobic treatment, and similarly incinerated or disposed of as industrial waste.
【０００４】[0004]
【発明が解決しようとしている問題点】上記嫌気性硝化
による余剰汚泥の従来の減量化においては、エネルギー
がメタンガスとして回収される等の利点があるが、硝化
に要する日数が２０〜４０日間と長く、そのうえ余剰汚
泥の分解率が６０％程度と低い為、広い敷地面積が要求
され、未分解余剰汚泥及びその他の固形物は脱水機等に
より分離され、焼却されるか或は産業廃棄物として処分
せねばならず、非効率で処理コストが大きくかかるとい
う問題がある。又、余剰汚泥を嫌気性硝化を行わずに脱
水機等により直接濃縮し、焼却或は産業廃棄物として処
分する場合には、余剰汚泥は減量化されていない為に、
更に処理コストが高くなるという問題がある。現在の汚
泥の処分費用は２〜３万円／ｍ3 と高く、更にこの処分
費は今後一層高騰する傾向にある。従って本発明の目的
は、活性汚泥方式で発生する余剰汚泥又は嫌気性硝化汚
泥等の有機性汚泥を効率良く減量化することが出来る方
法を提供することである。[Problems to be Solved by the Invention] The conventional reduction of excess sludge by anaerobic nitrification has the advantage that energy is recovered as methane gas, but the number of days required for nitrification is as long as 20 to 40 days. In addition, the decomposition rate of excess sludge is as low as about 60%, so a large site area is required, and undecomposed excess sludge and other solid matter are separated by a dehydrator, etc. and incinerated or disposed of as industrial waste. However, there is a problem that it is inefficient and the processing cost is high. Further, when the excess sludge is directly concentrated by a dehydrator or the like without performing anaerobic nitrification and incinerated or disposed of as industrial waste, the excess sludge is not reduced,
Further, there is a problem that the processing cost becomes high. The current sludge disposal cost is as high as 20,000 yen / m 3, and this disposal cost tends to rise further in the future. Therefore, an object of the present invention is to provide a method capable of efficiently reducing the amount of excess sludge generated by an activated sludge system or organic sludge such as anaerobic nitrifying sludge.
【０００５】[0005]
【問題点を解決する為の手段】上記目的は以下の本発明
によって達成される。即ち、本発明は、活性汚泥方式で
発生する汚泥の余剰部分或は嫌気性硝化汚泥等の有機性
汚泥を、金属イオンを触媒として酸化剤で酸化分解する
ことを特徴とする有機性汚泥の処理方法である。The above object can be achieved by the present invention described below. That is, the present invention is a treatment of an organic sludge characterized by oxidatively decomposing an excess sludge generated in an activated sludge system or an organic sludge such as an anaerobic nitrifying sludge with an oxidizing agent using a metal ion as a catalyst. Is the way.
【０００６】[0006]
【作用】排水を活性汚泥方式で処理して発生する汚泥の
余剰部分或は嫌気性硝化汚泥を、金属イオンを触媒とし
て酸化剤で酸化分解することにより、狭いスペースで短
時間で効率良く減量化することが出来る。[Function] The excess amount of sludge generated by treating wastewater by the activated sludge system or anaerobic nitrifying sludge is efficiently decomposed in a narrow space in a short time by oxidizing and decomposing it with an oxidizing agent using metal ions as a catalyst. You can do it.
【０００７】[0007]
【好ましい実施態様】次に好ましい実施態様を挙げて本
発明を更に詳細に説明する。本発明の好ましい１実施態
様は、図１又は図２に示す如き従来公知の排水処理方式
で発生する余剰汚泥又は嫌気性硝化汚泥を、図３に示す
如き酸化槽に移し、ここで該汚泥を必要なｐＨに調整し
て酸化剤及び触媒を添加し、余剰汚泥又は嫌気性硝化汚
泥を酸化分解する。尚、本発明の方法においては、酸化
処理前の汚泥を超音波処理して十分に解膠しておくこと
により、汚泥の酸化分解反応を著しく効率化することが
出来る。BEST MODE FOR CARRYING OUT THE INVENTION Next, the present invention will be described in more detail with reference to preferred embodiments. One preferred embodiment of the present invention is to transfer excess sludge or anaerobic nitrification sludge generated by a conventionally known wastewater treatment system as shown in FIG. 1 or FIG. 2 to an oxidation tank as shown in FIG. The required pH is adjusted and an oxidizing agent and a catalyst are added to oxidize and decompose excess sludge or anaerobic nitrifying sludge. In the method of the present invention, the oxidative decomposition reaction of sludge can be remarkably made efficient by subjecting the sludge before oxidization treatment to ultrasonic treatment to sufficiently deflocculate it.
【０００８】本発明において使用する酸化剤は、従来公
知の化学酸化方法において使用されている酸化剤、例え
ば、過酸化水素、過酸化カルシウム、過硫酸アンモニウ
ム、アルキルヒドロペルオキシド、過酸エステル、過酸
化ジアルキル又はジアシル等が使用されるが、コストや
副生成物等の点からみて過酸化水素が最も好ましい。以
下過酸化水素を代表例として説明する。過酸化水素の使
用量は、特に限定されず、余剰汚泥又は嫌気性硝化汚泥
の内容によって変化するが、好ましい使用量は余剰汚泥
又は嫌気性硝化汚泥１００重量部（固形分）に対して約
１０〜５００重量部（酸素として）となる範囲である。The oxidant used in the present invention is an oxidant used in a conventionally known chemical oxidation method, for example, hydrogen peroxide, calcium peroxide, ammonium persulfate, alkyl hydroperoxide, perester, dialkyl peroxide. Alternatively, diacyl or the like is used, but hydrogen peroxide is most preferable in terms of cost and by-products. Hereinafter, hydrogen peroxide will be described as a typical example. The amount of hydrogen peroxide used is not particularly limited and varies depending on the content of the excess sludge or the anaerobic nitrifying sludge, but the preferred amount is about 10 parts by weight per 100 parts by weight (solid content) of the excess sludge or the anaerobic nitrifying sludge. ˜500 parts by weight (as oxygen).
【０００９】本発明において使用する金属イオンとして
は、鉄、チタン、セリウム、銅、マンガン、コバルト、
バナジウム、クロム、鉛のイオン等が使用され、これら
の金属、金属酸化物、金属塩、錯体等いずれの形態でも
よい。本発明において特に好ましいものは鉄イオンであ
るので、以下鉄イオンを代表例として説明する。使用す
る鉄イオンは、従来技術においては第一鉄イオンが使用
されたが、本発明においては第一鉄イオンは勿論、第二
鉄イオンも有効であり、更に鉄屑等の如き金属鉄や鉄イ
オンをイオン交換樹脂等で固定した固定鉄イオンも使用
することが出来る。この触媒としての鉄イオンの使用量
は、過酸化水素１モル当たり約１０-3〜０．１モルで十
分な処理効果を挙げることが出来る。The metal ions used in the present invention include iron, titanium, cerium, copper, manganese, cobalt,
Ions of vanadium, chromium, lead, and the like are used, and any of these metals, metal oxides, metal salts, complexes, and the like may be used. Since iron ions are particularly preferable in the present invention, iron ions will be described below as a representative example. As the iron ion to be used, ferrous iron was used in the prior art, but ferrous ion as well as ferric ion is effective in the present invention, and further, metallic iron such as iron scrap or iron It is also possible to use fixed iron ions in which ions are fixed with an ion exchange resin or the like. The amount of iron ion used as the catalyst is about 10 −3 to 0.1 mol per mol of hydrogen peroxide, and sufficient treatment effect can be obtained.
【００１０】本発明方法では、余剰汚泥又は嫌気性硝化
汚泥の酸化は、反応液のｐＨを約２〜８に調節して行な
うことが好ましい。酸化反応は常温でもよいが、好まし
い範囲は４０℃〜１００℃、更に好ましくは５０℃〜８
０℃の範囲である。余剰汚泥又は嫌気性硝化汚泥の加熱
は、水蒸気等の吹込み、工場における他の温水等による
熱交換等、任意の加温手段を利用することが出来、加温
の方法は特に限定されない。In the method of the present invention, it is preferable to oxidize excess sludge or anaerobic nitrifying sludge by adjusting the pH of the reaction solution to about 2-8. The oxidation reaction may be carried out at room temperature, but the preferred range is 40 ° C to 100 ° C, more preferably 50 ° C to 8 ° C.
It is in the range of 0 ° C. The excess sludge or the anaerobic nitrifying sludge can be heated by using any heating means such as blowing in steam or heat exchange with other hot water in the factory, and the heating method is not particularly limited.
【００１１】処理温度が４０℃未満である場合には、酸
化に時間がかかり、酸化効率が不十分で且つ過酸化水素
の利用効率が不十分である。又、１００℃を越える温度
はそれ以上の処理効果を期待することが出来ず、又、過
酸化水素の自己分解が大きく、利用効率が低下すると共
に、加熱エネルギー消費が大になるだけで特別の利点は
ない。酸化反応時間は、酸化槽のサイズ、撹拌機の性
能、温度等によって異なるが、例えば、余剰汚泥又は嫌
気性硝化汚泥（固形分約１重量％）の量が１０ｍ3 で酸
化温度が５０℃で充分な撹拌が行われる場合には、約１
〜３時間の反応温度で充分であり、余剰汚泥又は嫌気性
硝化汚泥の約７０〜８０重量％を分解することが出来
る。When the treatment temperature is lower than 40 ° C., it takes time to oxidize, the oxidation efficiency is insufficient, and the utilization efficiency of hydrogen peroxide is insufficient. Further, if the temperature exceeds 100 ° C., no further treatment effect can be expected, and the self-decomposition of hydrogen peroxide is large, so that the utilization efficiency is lowered and the consumption of heating energy is large. There is no advantage. The oxidation reaction time varies depending on the size of the oxidation tank, the performance of the stirrer, the temperature, etc. For example, the amount of excess sludge or anaerobic nitrification sludge (solid content: about 1% by weight) is 10 m 3 , and the oxidation temperature is 50 ° C. Approximately 1 if sufficient agitation is provided
Reaction temperatures of up to 3 hours are sufficient and can decompose about 70-80% by weight of excess sludge or anaerobic nitrifying sludge.
【００１２】[0012]
【実施例】次に実施例を挙げて本発明を更に具体的に説
明する。 実施例１ 食品工場の排水を処理している排水処理施設の活性汚泥
（汚泥濃度１１，０００ｍｇ／リットル）を３００ｍｌ
のビーカーに１００ｍｌ取り、ｐＨ３に調整後、第一鉄
イオン２５０ｍｇ／リットル及び過酸化水素１０，００
０ｍｇ／リットルになる様に、夫々鉄分と過酸化水素水
を添加した。その後振とうしながら７０℃で１時間反応
させ、反応後の溶解性ＴＯＣ(Totalorganic carbon)と
残渣（不溶性ＴＯＣ）を測定したところ、処理前の溶解
性ＴＯＣは約２００ｍｇ／リットルで、不溶解性ＴＯＣ
の量は約６，０００ｍｇ／リットルであったが、処理後
の溶解性ＴＯＣは約４０００ｍｇ／リットルで、不溶解
性ＴＯＣの量は約１，８００ｍｇ／リットルであった。EXAMPLES Next, the present invention will be described more specifically with reference to examples. Example 1 300 ml of activated sludge (sludge concentration: 11,000 mg / liter) in a wastewater treatment facility that treats the wastewater of a food factory
Take 100 ml in a beaker and adjust to pH 3, ferrous ion 250 mg / liter and hydrogen peroxide 10,000
Iron content and hydrogen peroxide solution were added so that the amount became 0 mg / liter. After that, the mixture was reacted with shaking at 70 ° C for 1 hour, and the soluble TOC (Total organic carbon) and the residue (insoluble TOC) after the reaction were measured. The soluble TOC before the treatment was about 200 mg / liter, and the insoluble TOC
Was about 6,000 mg / liter, the soluble TOC after treatment was about 4000 mg / liter, and the amount of insoluble TOC was about 1,800 mg / liter.
【００１３】上記結果からして活性汚泥は、酸化により
全ＴＯＣの７０％が無機化或は可溶化することが明らか
である。この可溶化したＴＯＣは、曝気槽に戻して活性
汚泥により容易に生物分解することが出来るので、酸化
槽からの脱離液（上澄液）及び脱水機等からの濾過水を
曝気槽に戻すことにより、容易に生物分解が可能であ
る。不溶性ＴＯＣは、処理前のＴＯＣの約３０％程度と
なっており、脱水機等により脱水処理されて廃棄処分さ
れる。上記実験で得られた処理前の活性汚泥と処理後の
活性汚泥のＢＯＤとＴＯＣを測定したところ、下記表１
の通りであった。From the above results, it is clear that 70% of the total TOC in the activated sludge is mineralized or solubilized by oxidation. Since this solubilized TOC can be returned to the aeration tank and easily biodegraded by the activated sludge, the desorbed liquid (supernatant liquid) from the oxidation tank and the filtered water from the dehydrator etc. are returned to the aeration tank. Therefore, biodegradation can be easily performed. The insoluble TOC is about 30% of the TOC before the treatment, and it is dehydrated by a dehydrator or the like and discarded. The BOD and TOC of the activated sludge before treatment and the activated sludge after treatment obtained in the above experiment were measured, and the results are shown in Table 1 below.
It was the street.
【００１４】[0014]
【表１】 上記第１表からして、処理前のＢＯＤ／ＴＯＣは０．３
であり、処理後のＢＯＤ／ＴＯＣは１．３となり、本発
明方法によって発生したＢＯＤ分は曝気槽に戻して生物
分解可能であるので、最終的に処分される活性汚泥の量
は著しく減量化されている。[Table 1] From Table 1 above, BOD / TOC before treatment is 0.3.
The BOD / TOC after treatment is 1.3, and the BOD generated by the method of the present invention can be returned to the aeration tank and biodegraded, so that the amount of activated sludge finally disposed is significantly reduced. Has been done.
【００１５】実施例２ 実施例１で使用したと同じ活性汚泥をＳＴＲ３０日で高
温硝化を行っている嫌気性硝化汚泥（汚泥濃度１８，０
００ｍｇ／リットル）３００ｍｌのビーカーに１００ｍ
ｌ取り、ｐＨ３に調整後、第一鉄イオン２５０ｍｇ／リ
ットル及び過酸化水素２０，０００ｍｇ／リットルにな
る様に、夫々鉄分と過酸化水素水を添加した。その後、
振とうしながら５０℃で１時間反応させ、反応後の溶解
性ＴＯＣと不溶性ＴＯＣを測定したところ、処理前の溶
解性ＴＯＣは約２，０００ｍｇ／リットルで、不溶解性
ＴＯＣの量は約８，０００ｍｇ／リットルであったが、
処理後の溶解性ＴＯＣは約３，０００ｍｇ／リットル
で、不溶解性ＴＯＣの量は約４，０００ｍｇ／リットル
であった。Example 2 The same activated sludge as used in Example 1 was subjected to high temperature nitrification for 30 days in STR, and anaerobic nitrification sludge (sludge concentration: 18,0).
00mg / l) 100m in a 300ml beaker
After adjusting the pH to 3, the iron content and hydrogen peroxide solution were added so that the ferrous ion was 250 mg / liter and the hydrogen peroxide was 20,000 mg / liter. afterwards,
After reacting at 50 ° C for 1 hour with shaking, the soluble TOC and insoluble TOC after the reaction were measured. The soluble TOC before the treatment was about 2,000 mg / liter, and the amount of insoluble TOC was about 8 It was 1,000 mg / liter,
The soluble TOC after the treatment was about 3,000 mg / liter, and the amount of insoluble TOC was about 4,000 mg / liter.
【００１６】実施例３ 実施例１で使用したと同じ活性汚泥をＳＴＲ３０日で高
温硝化を行っている嫌気性硝化汚泥（汚泥濃度１８，０
００ｍｇ／リットル）３００ｍｌのビーカーに１００ｍ
ｌ取り、超音波発生器（出力２００Ｗ）にて１０分間解
膠処理後、ｐＨ３に調整し、第一鉄イオン２５０ｍｇ／
リットル及び過酸化水素２０，０００ｍｇ／リットルに
なる様に、夫々鉄分と過酸化水素水を添加した。その
後、振とうしながら５０℃で１時間反応させ、反応後の
溶解性ＴＯＣと不溶性ＴＯＣを測定したところ、処理前
の溶解性ＴＯＣは約２，０００ｍｇ／リットルで、不溶
解性ＴＯＣの量は約８，０００ｍｇ／リットルであった
が、処理後の溶解性ＴＯＣは約３，０００ｍｇ／リット
ルで、不溶解性ＴＯＣの量は約２，０００ｍｇ／リット
ルであった。上記の結果からして嫌気性硝化汚泥は、酸
化により不溶性ＴＯＣの５０重量％が無機化或は可溶化
することが明らかになった。又、前処理として嫌気性硝
化汚泥を超音波処理することにより、酸化により不溶性
ＴＯＣの７５重量％が無機化或は可溶化することが明ら
かになった。Example 3 The same activated sludge used in Example 1 was subjected to high temperature nitrification at STR 30 days for anaerobic nitrification sludge (sludge concentration 18,0).
00mg / l) 100m in a 300ml beaker
l, deflocculate with an ultrasonic generator (output 200W) for 10 minutes, adjust to pH 3, ferrous ion 250 mg /
Iron and hydrogen peroxide solution were added so that liter and hydrogen peroxide were 20,000 mg / liter, respectively. After that, the mixture was reacted with shaking at 50 ° C. for 1 hour, and the soluble TOC and insoluble TOC after the reaction were measured. The soluble TOC before the treatment was about 2,000 mg / liter, and the amount of insoluble TOC was Although it was about 8,000 mg / liter, the soluble TOC after the treatment was about 3,000 mg / liter, and the amount of insoluble TOC was about 2,000 mg / liter. From the above results, it was revealed that in the anaerobic nitrifying sludge, 50% by weight of insoluble TOC is mineralized or solubilized by oxidation. Further, it was revealed that 75% by weight of insoluble TOC was mineralized or solubilized by oxidation by ultrasonic treatment of anaerobic nitrification sludge as a pretreatment.
【００１７】[0017]
【効果】以上の如き本発明によれば、数時間の反応で高
い効率で余剰汚泥或は嫌気性硝化汚泥等の有機性汚泥を
減量化することが可能であり、従来技術における長時間
の硝化及び広いスペースを要し且つ減量化効率が低いと
いう問題が十分に解決された。[Effects] According to the present invention as described above, it is possible to highly efficiently reduce the amount of organic sludge such as excess sludge or anaerobic nitrification sludge by a reaction of several hours, and to perform nitrification for a long time in the conventional technique. In addition, the problems of requiring a large space and having a low weight reduction efficiency have been sufficiently solved.
【００１８】[0018]
【図１】活性汚泥法の標準的処理工程を図解的に説明す
る図FIG. 1 is a diagram schematically illustrating a standard treatment process of the activated sludge method.
【図２】嫌気性硝化処理工程を図解的に説明する図FIG. 2 is a diagram schematically illustrating an anaerobic nitrification treatment process.
【図３】本発明の方法を図解的に説明する図FIG. 3 is a diagram schematically illustrating the method of the present invention.
─────────────────────────────────────────────────────
─────────────────────────────────────────────────── ───
【手続補正書】[Procedure amendment]
【提出日】平成５年１２月１日[Submission date] December 1, 1993
【手続補正１】[Procedure Amendment 1]
【補正対象書類名】明細書[Document name to be amended] Statement
【補正対象項目名】全文[Correction target item name] Full text
【補正方法】変更[Correction method] Change
【補正内容】[Correction content]
【書類名】 明細書[Document name] Statement
【発明の名称】 有機性汚泥の処理方法[Title of Invention] Method for treating organic sludge
【特許請求の範囲】[Claims]
【発明の詳細な説明】Detailed Description of the Invention
【０００１】[0001]
【産業上の利用分野】本発明は有機性汚泥の処理方法に
関し、更に詳しくは排水を活性汚泥方式で処理して発生
する汚泥の余剰部分或は余剰汚泥の嫌気性消化で発生す
る嫌気性消化汚泥等の有機性汚泥を処理して、該汚泥を
減量化する有機性汚泥の処理方法に関する。BACKGROUND OF THE INVENTION This invention relates to method of treating organic sludge, more particularly anaerobic occurs in anaerobic digestion of the excess portion or excess sludge sludge produced by treating the waste water with activated sludge method digestion The present invention relates to a method for treating organic sludge such as sludge to reduce the amount of the sludge.
【０００２】[0002]
【従来の技術】従来、ＢＯＤで示される排水中の有機汚
濁成分の除去においては、現在実用化されている活性汚
泥方式等の生物学的処理方法によって、比較的低いコス
トで満足し得る結果が得られている。上記活性汚泥方式
では、図１に示す様に、処理対象排水を最初沈澱池に導
き、比重の重いものを沈澱させ、次いで曝気槽におい
て、活性汚泥によって排水中の有機物を分解させる。こ
の活性汚泥処理では、分解したＢＯＤのうちの５０〜７
０重量％は微生物の生活エネルギーに消費され、残りの
３０〜７０重量％は菌体の増殖に使用される為、余剰汚
泥が発生することになる。2. Description of the Related Art Conventionally, in the removal of organic pollutants in wastewater indicated by BOD, a biological treatment method such as an activated sludge system which has been put into practical use has been satisfactory at a relatively low cost. Has been obtained. In the activated sludge system, as shown in FIG. 1, the wastewater to be treated is first introduced into a settling tank to precipitate the one having a large specific gravity, and then the organic matter in the wastewater is decomposed by the activated sludge in the aeration tank. In this activated sludge treatment, 50 to 7 out of the decomposed BOD
Since 0% by weight is consumed for living energy of microorganisms and the remaining 30 to 70% by weight is used for the growth of bacterial cells, excess sludge is generated.
【０００３】活性汚泥処理で発生した余剰汚泥は、生物
難分解性であり且つ粘性が高いので、活性汚泥処理方式
では発生する余剰汚泥の処理が大きな問題となる。現
在、余剰汚泥の処理方法は、図２に示す様に、嫌気性消
化により、余剰汚泥をメタンガス、二酸化炭素、水素、
硫化水素等に分解して減量化し、その後分解されなかっ
た余剰汚泥及びその他の固形物は脱水機等により分離さ
れ、焼却されるか或は産業廃棄物として処分される。
又、場合によっては余剰汚泥は嫌気性処理を行わずに直
接脱水機等により分離され、同様に焼却されるか或は産
業廃棄物として処分される。Excess sludge generated by the activated sludge treatment is biodegradable and has a high viscosity, so that the treatment of the excess sludge generated in the activated sludge treatment system is a serious problem. Currently, the treatment methods of the excess sludge is, as shown in FIG. 2, anaerobic consumption
By the excess sludge methane gas, carbon dioxide, hydrogen,
Excess sludge and other solids that are not decomposed after being decomposed into hydrogen sulfide and the like to reduce the amount are separated by a dehydrator or the like and incinerated or disposed as industrial waste.
In some cases, excess sludge is directly separated by a dehydrator or the like without performing anaerobic treatment, and similarly incinerated or disposed of as industrial waste.
【０００４】[0004]
【発明が解決しようとしている問題点】上記嫌気性消化
による余剰汚泥の従来の減量化においては、エネルギー
がメタンガスとして回収される等の利点があるが、消化
に要する日数が２０〜４０日間と長く、そのうえ余剰汚
泥の分解率が６０％程度と低い為、広い敷地面積が要求
され、未分解余剰汚泥及びその他の固形物は脱水機等に
より分離され、焼却されるか或は産業廃棄物として処分
せねばならず、非効率で処理コストが大きくかかるとい
う問題がある。又、余剰汚泥を嫌気性消化を行わずに脱
水機等により直接濃縮し、焼却或は産業廃棄物として処
分する場合には、余剰汚泥は減量化されていない為に、
更に処理コストが高くなるという問題がある。現在の汚
泥の処分費用は２〜３万円／ｍ３と高く、更にこの処分
費は今後一層高騰する傾向にある。従って本発明の目的
は、活性汚泥方式で発生する余剰汚泥又は嫌気性消化汚
泥等の有機性汚泥を効率良く減量化することが出来る方
法を提供することである。Problems to be Solved by the Invention In the conventional reduction of excess sludge by anaerobic digestion, there is an advantage that energy is recovered as methane gas, but it is required for digestion. The number of days is as long as 20 to 40 days, and the decomposition rate of excess sludge is as low as about 60%, so a large site area is required, and undecomposed excess sludge and other solid matter are separated by a dehydrator and incinerated. Alternatively, it must be disposed of as industrial waste, which is inefficient and requires a large treatment cost. Also, when the excess sludge is directly concentrated by a dehydrator or the like without performing anaerobic digestion and incinerated or disposed of as industrial waste, the excess sludge is not reduced,
Further, there is a problem that the processing cost becomes high. The current sludge disposal cost is as high as 20,000 yen / m 3, and this disposal cost tends to rise further in the future. Therefore, an object of the present invention is to provide a method capable of efficiently reducing the amount of organic sludge such as surplus sludge or anaerobic digestion sludge generated by an activated sludge system.
【０００５】[0005]
【問題点を解決する為の手段】上記目的は以下の本発明
によって達成される。即ち、本発明は、活性汚泥方式で
発生する汚泥の余剰部分或は嫌気性消化汚泥等の有機性
汚泥を、金属イオンを触媒として酸化剤で酸化分解する
ことを特徴とする有機性汚泥の処理方法である。The above object can be achieved by the present invention described below. That is, the present invention is a treatment of an organic sludge characterized by oxidatively decomposing an excess sludge generated in an activated sludge system or an organic sludge such as an anaerobic digestion sludge with an oxidizing agent using a metal ion as a catalyst. Is the way.
【０００６】[0006]
【作用】排水を活性汚泥方式で処理して発生する汚泥の
余剰部分或は嫌気性消化汚泥を、金属イオンを触媒とし
て酸化剤で酸化分解することにより、狭いスペースで短
時間で効率良く減量化することが出来る。[Function] Efficient reduction in a narrow space in a short time by oxidizing and decomposing excess part of sludge or anaerobic digestion sludge generated by treating wastewater by activated sludge system with an oxidizing agent using a metal ion as a catalyst. You can do it.
【０００７】[0007]
【好ましい実施態様】次に好ましい実施態様を挙げて本
発明を更に詳細に説明する。本発明の好ましい１実施態
様は、図１又は図２に示す如き従来公知の排水処理方式
で発生する余剰汚泥又は嫌気性消化汚泥を、図３に示す
如き酸化槽に移し、ここで該汚泥を必要なｐＨに調整し
て酸化剤及び触媒を添加し、余剰汚泥又は嫌気性消化汚
泥を酸化分解する。尚、本発明の方法においては、酸化
処理前の汚泥を超音波処理して十分に解膠しておくこと
により、汚泥の酸化分解反応を著しく効率化することが
出来る。BEST MODE FOR CARRYING OUT THE INVENTION Next, the present invention will be described in more detail with reference to preferred embodiments. In a preferred embodiment of the present invention, excess sludge or anaerobic digested sludge generated by a conventionally known wastewater treatment system as shown in FIG. 1 or 2 is transferred to an oxidation tank as shown in FIG. The required pH is adjusted and an oxidizing agent and a catalyst are added to oxidize and decompose excess sludge or anaerobic digestion sludge. In the method of the present invention, the oxidative decomposition reaction of sludge can be remarkably made efficient by subjecting the sludge before oxidization treatment to ultrasonic treatment to sufficiently deflocculate it.
【０００８】本発明において使用する酸化剤は、従来公
知の化学酸化方法において使用されている酸化剤、例え
ば、過酸化水素、過酸化カルシウム、過硫酸アンモニウ
ム、アルキルヒドロペルオキシド、過酸エステル、過酸
化ジアルキル又はジアシル等が使用されるが、コストや
副生成物等の点からみて過酸化水素が最も好ましい。以
下過酸化水素を代表例として説明する。過酸化水素の使
用量は、特に限定されず、余剰汚泥又は嫌気性消化汚泥
の内容によって変化するが、好ましい使用量は余剰汚泥
又は嫌気性消化汚泥１００重量部（固形分）に対して約
１０〜５００重量部（酸素として）となる範囲である。The oxidant used in the present invention is an oxidant used in a conventionally known chemical oxidation method, for example, hydrogen peroxide, calcium peroxide, ammonium persulfate, alkyl hydroperoxide, perester, dialkyl peroxide. Alternatively, diacyl or the like is used, but hydrogen peroxide is most preferable in terms of cost and by-products. Hereinafter, hydrogen peroxide will be described as a typical example. The amount of hydrogen peroxide used is not particularly limited and varies depending on the content of the excess sludge or the anaerobic digested sludge, but the preferred amount of hydrogen peroxide is about 10 parts by weight per 100 parts by weight (solid content) of the excess sludge or the anaerobic digested sludge. ˜500 parts by weight (as oxygen).
【０００９】本発明において使用する金属イオンとして
は、鉄、チタン、セリウム、銅、マンガン、コバルト、
バナジウム、クロム、鉛のイオン等が使用され、これら
の金属、金属酸化物、金属塩、錯体等いずれの形態でも
よい。本発明において特に好ましいものは鉄イオンであ
るので、以下鉄イオンを代表例として説明する。使用す
る鉄イオンは、従来技術においては第一鉄イオンが使用
されたが、本発明においては第一鉄イオンは勿論、第二
鉄イオンも有効であり、更に鉄屑等の如き金属鉄や鉄イ
オンをイオン交換樹脂等で固定した固定鉄イオンも使用
することが出来る。この触媒としての鉄イオンの使用量
は、過酸化水素１モル当たり約１０-3〜０．１モルで十
分な処理効果を挙げることが出来る。The metal ions used in the present invention include iron, titanium, cerium, copper, manganese, cobalt,
Ions of vanadium, chromium, lead, and the like are used, and any of these metals, metal oxides, metal salts, complexes, and the like may be used. Since iron ions are particularly preferable in the present invention, iron ions will be described below as a representative example. As the iron ion to be used, ferrous iron was used in the prior art, but ferrous ion as well as ferric ion is effective in the present invention, and further, metallic iron such as iron scrap or iron It is also possible to use fixed iron ions in which ions are fixed with an ion exchange resin or the like. The amount of iron ion used as the catalyst is about 10 −3 to 0.1 mol per mol of hydrogen peroxide, and sufficient treatment effect can be obtained.
【００１０】本発明方法では、余剰汚泥又は嫌気性消化
汚泥の酸化は、反応液のｐＨを約２〜８に調節して行な
うことが好ましい。酸化反応は常温でもよいが、好まし
い範囲は４０℃〜１００℃、更に好ましくは５０℃〜８
０℃の範囲である。余剰汚泥又は嫌気性消化汚泥の加熱
は、水蒸気等の吹込み、工場における他の温水等による
熱交換等、任意の加温手段を利用することが出来、加温
の方法は特に限定されない。In the method of the present invention, it is preferable to oxidize excess sludge or anaerobic digestion sludge by adjusting the pH of the reaction solution to about 2-8. The oxidation reaction may be carried out at room temperature, but the preferred range is 40 ° C to 100 ° C, more preferably 50 ° C to 8 ° C.
It is in the range of 0 ° C. For heating the excess sludge or the anaerobic digested sludge, any heating means such as blowing of steam or heat exchange with other hot water in the factory can be used, and the heating method is not particularly limited.
【００１１】処理温度が４０℃未満である場合には、酸
化に時間がかかり、酸化効率が不十分で且つ過酸化水素
の利用効率が不十分である。又、１００℃を越える温度
はそれ以上の処理効果を期待することが出来ず、又、過
酸化水素の自己分解が大きく、利用効率が低下すると共
に、加熱エネルギー消費が大になるだけで特別の利点は
ない。酸化反応時間は、酸化槽のサイズ、撹拌機の性
能、温度等によって異なるが、例えば、余剰汚泥又は嫌
気性消化汚泥（固形分約１重量％）の量が１０ｍ3 で酸
化温度が５０℃で充分な撹拌が行われる場合には、約１
〜３時間の反応温度で充分であり、余剰汚泥又は嫌気性
消化汚泥の約７０〜８０重量％を分解することが出来
る。When the treatment temperature is lower than 40 ° C., it takes time to oxidize, the oxidation efficiency is insufficient, and the utilization efficiency of hydrogen peroxide is insufficient. Further, if the temperature exceeds 100 ° C., no further treatment effect can be expected, and the self-decomposition of hydrogen peroxide is large, so that the utilization efficiency is lowered and the consumption of heating energy is large. There is no advantage. Although the oxidation reaction time varies depending on the size of the oxidation tank, the performance of the stirrer, the temperature, etc., for example, the amount of excess sludge or anaerobic digestion sludge (solid content: about 1% by weight) is 10 m 3 , and the oxidation temperature is 50 ° C. Approximately 1 if sufficient agitation is provided
~ 3 hours reaction temperature is sufficient, excess sludge or anaerobic
About 70 to 80% by weight of digested sludge can be decomposed.
【００１２】[0012]
【実施例】次に実施例を挙げて本発明を更に具体的に説
明する。 実施例１ 食品工場の排水を処理している排水処理施設の活性汚泥
（汚泥濃度１１，０００ｍｇ／リットル）を３００ｍｌ
のビーカーに１００ｍｌ取り、ｐＨ３に調整後、第一鉄
イオン２５０ｍｇ／リットル及び過酸化水素１０，００
０ｍｇ／リットルになる様に、夫々鉄分と過酸化水素水
を添加した。その後振とうしながら７０℃で１時間反応
させ、反応後の溶解性ＴＯＣ（Ｔｏｔａｌ ｏｒｇａｎ
ｉｃ ｃａｒｂｏｎ）と残渣（不溶性ＴＯＣ）を測定し
たところ、処理前の溶解性ＴＯＣは約２００ｍｇ／リッ
トルで、不溶解性ＴＯＣの量は約６，０００ｍｇ／リッ
トルであったが、処理後の溶解性ＴＯＣは約４０００ｍ
ｇ／リットルで、不溶解性ＴＯＣの量は約１，８００ｍ
ｇ／リットルであった。EXAMPLES Next, the present invention will be described more specifically with reference to examples. Example 1 300 ml of activated sludge (sludge concentration: 11,000 mg / liter) in a wastewater treatment facility that treats the wastewater of a food factory
Take 100 ml in a beaker and adjust to pH 3, ferrous ion 250 mg / liter and hydrogen peroxide 10,000
Iron content and hydrogen peroxide solution were added so that the amount became 0 mg / liter. After that, the mixture was reacted with shaking at 70 ° C. for 1 hour, and the soluble TOC (Total organo
ic carbon) and the residue (insoluble TOC) were measured, the soluble TOC before treatment was about 200 mg / liter and the amount of insoluble TOC was about 6,000 mg / liter, but the solubility after treatment was TOC is about 4000m
The amount of insoluble TOC is about 1,800 m in g / liter
It was g / liter.
【００１３】上記結果からして活性汚泥は、酸化により
全ＴＯＣの７０％が無機化或は可溶化することが明らか
である。この可溶化したＴＯＣは、曝気槽に戻して活性
汚泥により容易に生物分解することが出来るので、酸化
槽からの脱離液（上澄液）及び脱水機等からの濾過水を
曝気槽に戻すことにより、容易に生物分解が可能であ
る。不溶性ＴＯＣは、処理前のＴＯＣの約３０％程度と
なっており、脱水機等により脱水処理されて廃棄処分さ
れる。上記実験で得られた処理前の活性汚泥と処理後の
活性汚泥のＢＯＤとＴＯＣを測定したところ、下記表１
の通りであった。From the above results, it is clear that 70% of the total TOC in the activated sludge is mineralized or solubilized by oxidation. Since this solubilized TOC can be returned to the aeration tank and easily biodegraded by the activated sludge, the desorbed liquid (supernatant liquid) from the oxidation tank and the filtered water from the dehydrator etc. are returned to the aeration tank. Therefore, biodegradation can be easily performed. The insoluble TOC is about 30% of the TOC before the treatment, and it is dehydrated by a dehydrator or the like and discarded. The BOD and TOC of the activated sludge before treatment and the activated sludge after treatment obtained in the above experiment were measured, and the results are shown in Table 1 below.
It was the street.
【００１４】[0014]
【表１】 上記第１表からして、処理前のＢＯＤ／ＴＯＣは０．３
であり、処理後のＢＯＤ／ＴＯＣは１．３となり、本発
明方法によって発生したＢＯＤ分は曝気槽に戻して生物
分解可能であるので、最終的に処分される活性汚泥の量
は著しく減量化されている。[Table 1] From Table 1 above, BOD / TOC before treatment is 0.3.
The BOD / TOC after treatment is 1.3, and the BOD generated by the method of the present invention can be returned to the aeration tank and biodegraded, so that the amount of activated sludge finally disposed is significantly reduced. Has been done.
【００１５】実施例２ 実施例１で使用したと同じ活性汚泥をＳＴＲ３０日で高
温消化を行っている嫌気性消化汚泥（汚泥濃度１８，０
００ｍｇ／リットル）を３００ｍｌのビーカーに１００
ｍｌ取り、ｐＨ３に調整後、第一鉄イオン２５０ｍｇ／
リットル及び過酸化水素２０，０００ｍｇ／リットルに
なる様に、夫々鉄分と過酸化水素水を添加した。その
後、振とうしながら５０℃で１時間反応させ、反応後の
溶解性ＴＯＣと不溶性ＴＯＣを測定したところ、処理前
の溶解性ＴＯＣは約２，０００ｍｇ／リットルで、不溶
解性ＴＯＣの量は約８，０００ｍｇ／リットルであった
が、処理後の溶解性ＴＯＣは約３，０００ｍｇ／リット
ルで、不溶解性ＴＯＣの量は約４，０００ｍｇ／リット
ルであった。[0015] Example 2 The same activated sludge as used in Example 1 is carried out STR30_nichidekoon digestion anaerobic digestion sludge (sludge concentration 18,0
00mg / l) 100 in a 300ml beaker
After taking up ml and adjusting to pH 3, ferrous ion 250 mg /
Iron and hydrogen peroxide solution were added so that liter and hydrogen peroxide were 20,000 mg / liter, respectively. After that, the mixture was reacted with shaking at 50 ° C. for 1 hour, and the soluble TOC and insoluble TOC after the reaction were measured. The soluble TOC before the treatment was about 2,000 mg / liter, and the amount of insoluble TOC was Although it was about 8,000 mg / liter, the soluble TOC after the treatment was about 3,000 mg / liter and the amount of insoluble TOC was about 4,000 mg / liter.
【００１６】実施例３ 実施例１で使用したと同じ活性汚泥をＳＴＲ３０日で高
温消化を行っている嫌気性消化汚泥（汚泥濃度１８，０
００ｍｇ／リットル）を３００ｍｌのビーカーに１００
ｍｌ取り、超音波発生器（出力２００Ｗ）にて１０分間
解膠処理後、ｐＨ３に調整し、第一鉄イオン２５０ｍｇ
／リットル及び過酸化水素２０，０００ｍｇ／リットル
になる様に、夫々鉄分と過酸化水素水を添加した。その
後、振とうしながら５０℃で１時間反応させ、反応後の
溶解性ＴＯＣと不溶性ＴＯＣを測定したところ、処理前
の溶解性ＴＯＣは約２，０００ｍｇ／リットルで、不溶
解性ＴＯＣの量は約８，０００ｍｇ／リットルであった
が、処理後の溶解性ＴＯＣは約３，０００ｍｇ／リット
ルで、不溶解性ＴＯＣの量は約２，０００ｍｇ／リット
ルであった。上記の結果からして嫌気性消化汚泥は、酸
化により不溶性ＴＯＣの５０重量％が無機化或は可溶化
することが明らかになった。又、前処理として嫌気性消
化汚泥を超音波処理することにより、酸化により不溶性
ＴＯＣの７５重量％が無機化或は可溶化することが明ら
かになった。[0016] Example 3 The same activated sludge as used in Example 1 is carried out STR30_nichidekoon digestion anaerobic digestion sludge (sludge concentration 18,0
00mg / l) 100 in a 300ml beaker
Take ml and deflocculate for 10 minutes with an ultrasonic generator (output 200W), adjust to pH 3 and ferrous ion 250mg
/ Liter and hydrogen peroxide of 20,000 mg / liter were added with iron and hydrogen peroxide water, respectively. After that, the mixture was reacted with shaking at 50 ° C. for 1 hour, and the soluble TOC and insoluble TOC after the reaction were measured. The soluble TOC before the treatment was about 2,000 mg / liter, and the amount of insoluble TOC was Although it was about 8,000 mg / liter, the soluble TOC after the treatment was about 3,000 mg / liter, and the amount of insoluble TOC was about 2,000 mg / liter. From the above results, it was revealed that in the anaerobic digested sludge, 50% by weight of insoluble TOC is mineralized or solubilized by oxidation. Also, as pretreatment, anaerobic elimination
It was clarified that 75% by weight of insoluble TOC was mineralized or solubilized by oxidation by subjecting the activated sludge to ultrasonic treatment.
【００１７】[0017]
【効果】以上の如き本発明によれば、数時間の反応で高
い効率で余剰汚泥或は嫌気性消化汚泥等の有機性汚泥を
減量化することが可能であり、従来技術における長時間
の消化及び広いスペースを要し且つ減量化効率が低いと
いう問題が十分に解決された。[Effect] According to the present invention as described above, it is possible to reduce the amount of organic sludge such as excess sludge or anaerobic digestion sludge with a high efficiency in a reaction of several hours, and to digest for a long time in the conventional technique. In addition, the problems of requiring a large space and having a low weight reduction efficiency have been sufficiently solved.
【００１８】[0018]
【図面の簡単な説明】[Brief description of drawings]
【図１】活性汚泥法の標準的処理工程を図解的に説明す
る図FIG. 1 is a diagram schematically illustrating a standard treatment process of the activated sludge method.
【図２】嫌気性消化処理工程を図解的に説明する図FIG. 2 is a diagram schematically illustrating an anaerobic digestion treatment process.
【図３】本発明の方法を図解的に説明する図FIG. 3 is a diagram schematically illustrating the method of the present invention.
【手続補正３】[Procedure 3]
【補正対象書類名】図面[Document name to be corrected] Drawing
【補正対象項目名】全図[Correction target item name] All drawings
【補正方法】変更[Correction method] Change
【補正内容】[Correction content]
【図１】 [Figure 1]
【図２】 [Fig. 2]
【図３】 [Figure 3]
───────────────────────────────────────────────────── フロントページの続き (72)発明者 山本 一郎 東京都千代田区鍛冶町１−５−７ 環境エ ンジニアリング株式会社内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Ichiro Yamamoto 1-5-7 Kajimachi, Chiyoda-ku, Tokyo Inside Environmental Engineering Co., Ltd.
Claims (4)
或は嫌気性硝化汚泥等の有機性汚泥を、金属イオンを触
媒として酸化剤で酸化分解することを特徴とする有機性
汚泥の処理方法。1. A method for treating organic sludge, which comprises oxidatively decomposing an excess portion of sludge generated by an activated sludge system or an organic sludge such as anaerobic nitrifying sludge with an oxidizing agent using a metal ion as a catalyst. .
剤が過酸化水素である請求項１に記載の有機性汚泥の処
理方法。2. The method for treating organic sludge according to claim 1, wherein the metal ions are iron ions and the oxidizing agent is hydrogen peroxide.
囲に調整して加熱下に行う請求項１又は２に記載の有機
性汚泥の処理方法。3. The method for treating organic sludge according to claim 1 or 2, wherein the oxidation treatment is carried out under heating by adjusting the pH of the reaction solution within a range of 2 to 8.
る請求項１〜３に記載の有機性汚泥の処理方法。4. The method for treating organic sludge according to claim 1, wherein the organic sludge is subjected to ultrasonic treatment before the oxidation treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19675593A JP3489856B2 (en) | 1993-07-15 | 1993-07-15 | Organic sludge treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19675593A JP3489856B2 (en) | 1993-07-15 | 1993-07-15 | Organic sludge treatment method |
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| Publication Number | Publication Date |
|---|---|
| JPH0724499A true JPH0724499A (en) | 1995-01-27 |
| JP3489856B2 JP3489856B2 (en) | 2004-01-26 |
Family
ID=16363079
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP19675593A Expired - Lifetime JP3489856B2 (en) | 1993-07-15 | 1993-07-15 | Organic sludge treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3489856B2 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19639716A1 (en) * | 1996-09-26 | 1998-04-02 | Ciba Geigy Ag | Process for treating sludge in biological wastewater treatment |
| KR100324473B1 (en) * | 1999-03-31 | 2002-02-27 | 박형재 | A method making use of ultrasonic wave for treating waste water |
| JP2005334886A (en) * | 2005-08-23 | 2005-12-08 | Kobelco Eco-Solutions Co Ltd | Activated sludge treatment method and activated sludge treatment apparatus therefor |
| JP2005334713A (en) * | 2004-05-24 | 2005-12-08 | Mitsui Eng & Shipbuild Co Ltd | Treatment method and treatment system for treating fermentation residue liquid and other anaerobic organic compound-containing liquid |
| JP2013220378A (en) * | 2012-04-16 | 2013-10-28 | Shikoku Chem Corp | Volume reduction method for excess sludge |
| CN105712601A (en) * | 2014-12-04 | 2016-06-29 | 中国石油化工股份有限公司 | Method for treating residual activated sludge by catalyzing ozone |
| CN106277660A (en) * | 2015-05-18 | 2017-01-04 | 中国石油化工股份有限公司 | A kind of heterogeneous catalysis ozone processes the method for residual active sludge |
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| CN111977936B (en) * | 2020-07-15 | 2022-04-22 | 华南理工大学 | Method for grading, upgrading and recycling comprehensive utilization of oily sludge |
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1993
- 1993-07-15 JP JP19675593A patent/JP3489856B2/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19639716A1 (en) * | 1996-09-26 | 1998-04-02 | Ciba Geigy Ag | Process for treating sludge in biological wastewater treatment |
| EP0832853A3 (en) * | 1996-09-26 | 1998-05-27 | Ciba SC Holding AG | Process for the treatment of sludges from biological waste water treatment |
| KR100324473B1 (en) * | 1999-03-31 | 2002-02-27 | 박형재 | A method making use of ultrasonic wave for treating waste water |
| JP2005334713A (en) * | 2004-05-24 | 2005-12-08 | Mitsui Eng & Shipbuild Co Ltd | Treatment method and treatment system for treating fermentation residue liquid and other anaerobic organic compound-containing liquid |
| JP4488794B2 (en) * | 2004-05-24 | 2010-06-23 | 三井造船株式会社 | Method and system for treating fermentation residual liquid and other anaerobic organic compound-containing liquid |
| JP2005334886A (en) * | 2005-08-23 | 2005-12-08 | Kobelco Eco-Solutions Co Ltd | Activated sludge treatment method and activated sludge treatment apparatus therefor |
| JP2013220378A (en) * | 2012-04-16 | 2013-10-28 | Shikoku Chem Corp | Volume reduction method for excess sludge |
| CN105712601A (en) * | 2014-12-04 | 2016-06-29 | 中国石油化工股份有限公司 | Method for treating residual activated sludge by catalyzing ozone |
| CN105712601B (en) * | 2014-12-04 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of method of catalysis ozone processing residual active sludge |
| CN106277660A (en) * | 2015-05-18 | 2017-01-04 | 中国石油化工股份有限公司 | A kind of heterogeneous catalysis ozone processes the method for residual active sludge |
| CN117447038A (en) * | 2023-12-22 | 2024-01-26 | 南京大学 | Method for promoting anaerobic methane production of excess sludge by using iron-calcium combined pretreatment |
| CN117447038B (en) * | 2023-12-22 | 2024-04-09 | 南京大学 | Method for promoting anaerobic methane production of excess sludge by using iron-calcium combined pretreatment |
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| Publication number | Publication date |
|---|---|
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