JPH02277597A - Treatment of organic sewage - Google Patents
Treatment of organic sewageInfo
- Publication number
- JPH02277597A JPH02277597A JP1095423A JP9542389A JPH02277597A JP H02277597 A JPH02277597 A JP H02277597A JP 1095423 A JP1095423 A JP 1095423A JP 9542389 A JP9542389 A JP 9542389A JP H02277597 A JPH02277597 A JP H02277597A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- tank
- sewage
- treatment
- org
- 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 20
- 239000010802 sludge Substances 0.000 claims abstract description 107
- 238000000034 method Methods 0.000 claims abstract description 23
- 238000000926 separation method Methods 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 4
- 239000011707 mineral Substances 0.000 claims description 4
- 239000005416 organic matter Substances 0.000 claims description 2
- 238000005273 aeration Methods 0.000 abstract description 17
- 230000003381 solubilizing effect Effects 0.000 abstract description 3
- 230000001546 nitrifying effect Effects 0.000 abstract 1
- 230000000717 retained effect Effects 0.000 abstract 1
- 238000005063 solubilization Methods 0.000 description 20
- 230000007928 solubilization Effects 0.000 description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 238000004062 sedimentation Methods 0.000 description 7
- 239000007787 solid Substances 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000010800 human waste Substances 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
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 210000003850 cellular structure Anatomy 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
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 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
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 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
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000006228 supernatant 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)
- Treatment Of Sludge (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、０．６〜０．８
ｋｇ５ｓ／除去ＢＵＤ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、離脱水性であるため、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 must be treated by dehydration, drying, incineration, disposal, etc. It was previously disposed of through sludge treatment, but this process requires a large amount of expense and equipment costs. The amount of surplus sludge generated by the conventional activated sludge method is 0.6 to 0.8 per BOD removed.
kg5s/BUD removed, and it is well known that a very large amount of surplus sludge is generated. Moreover, since the surplus sludge is water-based in quality, it is becoming increasingly difficult to treat the sludge.
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、し尿、下水な
どの有機性汚水を、生物学的硝化脱窒法などの好気性生
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
鉱酸を添加し、ｐｆ１２．５以下、温度５０℃以上の加
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としたものである。In order to achieve the above object, in the present invention, organic wastewater such as human waste and sewage is subjected to aerobic biological treatment such as biological nitrification and denitrification, followed by solid-liquid separation, and the solid-liquid separated sludge is A portion of the sludge is returned to the biological treatment tank, while mineral acid is added to the other portion of the sludge, and the organic matter in the sludge is solubilized by retaining it under heated conditions of pf 12.5 or lower and temperature 50°C or higher. The method of treating organic wastewater is characterized by supplying the organic wastewater 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.
第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３
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。FIG. 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, is aerated for a predetermined time in the coexistence of BOD assimilation activated sludge, and then flows into the settling tank 3.
The activated sludge flows into the water, the activated sludge settles, and becomes clear treated water 4. 5 is a water sprinkler device.
沈殿槽のかわりに他の固液分離手段、例えば遠心分離、
浮上分離、ＵＰ膜又はＭＦ膜の膜分離でもかまわない。Instead of settling tanks, other solid-liquid separation means, such as centrifugation,
Floating separation, UP membrane or MF membrane separation may also be used.
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 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６の大部分は、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ＭＬＳＳ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
１５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ＨＣＩ
、１（２ＳＯ，などの鉱酸１２を汚泥可溶化槽１１に添
加し、ｐＨ２，５以下（好ましくはｐＨ１〜２）として
、所要時間（通常４〜２４ｈｒ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、５０℃
以上に加温（５０〜１００℃が好適）するのが重要であ
る。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 6 is transferred from the return sludge pipe 7 to the aeration tank 2.
The MLSS 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%. Afterwards, a part of the concentrated sludge 10 is led to a sludge dewatering step 15, and the other part is supplied to a sludge solubilization tank 11 (sometimes referred to as a sludge hydrolysis tank). and H.C.I.
, 1 (2SO, etc.) is added to the sludge solubilization tank 11 to adjust the pH to 2.5 or less (preferably pH 1 to 2) for the required time (usually 4 to 24 hr, the required time varies depending on the quality of the sludge). The temperature of the sludge solubilization tank 11 is set at 50°C to accelerate the solubilization (hydrolysis) rate.
It is important to heat the mixture to a temperature higher than 50 to 100° C. (preferably 50 to 100° C.). 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種々の微
生物の細胞構成成分（ポリサッカライド、プロティン、
脂質など）が、強酸性条件下で加水分解されて低分子化
され、分子量数千〜致方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濃度のＢ
ＯＤ成分を含むことも認められた。また、汚泥の一部は
可溶化されずに、Ｓｓ状のままで残る現象も認められた
。１７は加熱器であり、１３は濃縮工程分離水である。In the solubilization tank 11, cell components of various microorganisms (polysaccharides, proteins,
Analysis by gel chromatography has revealed that under strongly acidic conditions, lipids, etc.) are hydrolyzed and reduced in molecular weight, and are solubilized to a molecular colloidal state with a molecular weight of several thousand to several thousand. Solubilized sludge has a high concentration of B
It was also recognized that it contained an OD component. Furthermore, a phenomenon was observed in which a portion of the sludge was not solubilized and remained in the Ss state. 17 is a heater, and 13 is water separated from the concentration process.
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Ｈ
ＣＩ 、Ｈ，ＳＯ，などの鉱酸の所要量が、汚泥濃縮度
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、薬品コスト
的に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 H supplied to the sludge solubilization tank 11
Since the required amount of mineral acids such as CI, H, SO, etc. increases in inverse proportion to the degree of sludge concentration, it is recommended to supply sludge with a high solids concentration to the solubilization tank 11 as much as possible in order to reduce chemical costs. This is because it is desirable for
酸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、ＣＤ２
と８２０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Ｂ
ＯＤ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 acid is supplied to the aeration tank 2 or the sludge return line 7, and the activated sludge present in the aeration tank 2 reduces CD2.
and 820 biologically degraded. Of course, aeration tank 2
The BOD load is the BOD of influent sewage and the BOD of solubilized sludge.
It is important to design based on the total amount of OD and 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困
難な場合が多いので、曝気槽の肛ＳＳ濃度を高めること
によって対応したほうが好ましい。Note that when applying the present invention to an existing activated sludge process, it is often difficult to increase the capacity of the existing aeration tank 2, so it is better to deal with this by increasing the SS concentration in the aeration tank. preferable.
以上が本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、八〜′７４に減少すること
が確認された。また、下水、し尿などには粘土分などの
無機性のｓｓあるいは紙などの繊維分なども含まれてい
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。１６は汚泥脱水ケ
ーキである。The above is the treatment process of the present invention, and the inventor's long-run test over 6 months confirmed that the amount of surplus sludge generated was reduced by 8 to 74 mm compared to the conventional activated sludge method. It was done. In addition, sewage, human waste, etc. contain inorganic SS such as clay and fibers such as paper, so it is impossible for the amount of surplus sludge generated to be zero. 10' and sludge dewatering machine 15
Make sure to dehydrate it. 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（Ｂ ＯＤ １２０〜１８０ ｍｇ／ Ｉ
ｌ 、 ５Ｓ１００〜１５５ ｍｇ／ Ｉｌ ）を曝気
時間８ｈｒ、活性汚泥ＭＬＳＳ １８００〜２５００ｍ
ｇ／ Ｉｔの曝気槽（８００−ＭＬＳＳ負荷０．１８〜
０．２５ （ｋｇＢＯＤ ／ ｋｇ）ＭＬＳＳ ・日）
１．１ｍ供給したのち、水面積負荷１２ｍ’／ｍ２
・日の沈殿槽において、活性汚泥を沈降分離し、固形物
濃度１〜１．５％の沈殿汚泥を得た。Example 1 Initial settling overflow sewage (B OD 120-180 mg/I
l, 5S100-155 mg/Il) for aeration time 8 hr, activated sludge MLSS 1800-2500 m
g/It aeration tank (800-MLSS load 0.18 ~
0.25 (kgBOD/kg)MLSS・day)
After supplying 1.1m, water area load 12m'/m2
・Activated sludge was separated by sedimentation in a sedimentation tank to obtain precipitated sludge with a solids concentration of 1 to 1.5%.
下水処理量をＱ ｍ’／日とするとき、沈殿汚泥の０．
０１Ｑｍ’／日を遠心分離機による汚泥濃縮工程に供給
し、残りの沈殿汚泥は曝気槽に返送した。When the amount of sewage treated is Q m'/day, the amount of settled sludge is 0.
01 Qm'/day was supplied to the sludge concentration process using a centrifuge, and the remaining settled sludge was returned to the aeration tank.
遠心分離機（巴工業製、シャープレスＢＤ型スーパデカ
ンタ−）により、沈殿汚泥を濃縮したところ、固形物濃
度平均５．５％の濃縮汚泥を得た。When the precipitated sludge was concentrated using a centrifuge (manufactured by Tomoe Kogyo, Sharpless BD type super decanter), concentrated sludge with an average solid content of 5.5% was obtained.
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、硫酸を汚泥可溶化槽内液に対
し、ｐＨ１〜２．５になるように添加して、攪拌しなが
ら汚泥の可溶化（加水分解）を行った。しかるのち、可
溶化汚泥（Ｓ Ｓ ５６００〜６７００ｍｇ／ ｌ
ＳＢ ＯＤ ７５００〜９２００ｍｇ／ Ａ’ ）を、
前記の曝気槽に添加して、好気性、生物処理を行った。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.
Sulfuric acid was added to the liquid in the sludge solubilization tank to adjust the pH to 1 to 2.5 while heating the tank to 0 to 75°C, and the sludge was solubilized (hydrolyzed) while stirring. After that, solubilized sludge (SS 5600-6700 mg/l
SB OD 7500-9200mg/A'),
It was added to the aeration tank to perform aerobic and biological treatment.
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ＢＯＤ１５〜１８．５Ｓ２０〜２５ｍｇ
／ｊ！であった。また、余剰汚泥、発生量の６ケ月間の
変動範囲は下水処理量ｌｌＴ１３あたり、０．０３８〜
０．０４５ ｋｇｓｓであった。また沈殿槽に流入する
活性汚泥のＳＶＩ値は１５０〜２００であった。As a result of continuing operation according to the above conditions for 6 months, the water quality of the sedimentation tank effluent was BOD15-18.5S20-25mg
/j! Met. In addition, the fluctuation range of surplus sludge and generation amount over a six-month period is from 0.038 to 13 per sewage treatment volume 13
It was 0.045 kgss. Moreover, the SVI value of the activated sludge flowing into the settling tank was 150 to 200.
実施例２ 可溶化槽のｐＨと汚泥可溶化率の関係を第２図に示す。Example 2 Figure 2 shows the relationship between the pH of the solubilization tank and the sludge solubilization rate.
第２図において、原汚泥は固形物濃度４．８％の下水の
余剰活性汚泥を用いた。処理条件は温度８０℃、滞留時
間：２４ｈｒ一定とした。In FIG. 2, surplus activated sludge of sewage with a solids concentration of 4.8% was used as the raw sludge. The processing conditions were a constant temperature of 80° C. and a residence time of 24 hours.
汚泥可溶化率は、回分遠心分離機で１ｏ分間遠心分離し
、上澄液をすて、残りの汚泥の重量を測定し、次式で計
算した値である。The sludge solubilization rate is a value calculated using the following formula after centrifuging the sludge for 10 minutes using a batch centrifuge, discarding the supernatant, and measuring the weight of the remaining sludge.
実施例３
次に、可溶化槽の温度と可溶化率との関係を調べた結果
を第３図に示す。ｐＨは１．５一定、滞留時間は２４ｈ
ｒ一定とした。原汚泥の種類と濃度は実施例２と同一で
ある。Example 3 Next, FIG. 3 shows the results of investigating the relationship between the temperature of the solubilization tank and the solubilization rate. pH is constant 1.5, residence time is 24 hours
r was set constant. The type and concentration of raw sludge are the same as in Example 2.
第２図及び第３図の結果より、ｐＨは２．５以下、温度
５０℃以上が酸による汚泥の可溶化に好適な条件である
ことが認められた。From the results shown in FIGS. 2 and 3, it was recognized that pH of 2.5 or lower and temperature of 50° C. or higher are suitable conditions for solubilizing sludge with acid.
比較例
第１図の本発明フローの、汚泥可溶化槽、硫酸の添加を
省略した以外は、同一条件（下水処理量、流入下水水質
、曝気槽滞留時間、ＢＵＤ−３Ｓ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（７）ＳＶＩは１８０〜２７０ 、
沈殿流出水のＢＯＤ１２〜２０．５Ｓ２８〜３５ｍｇ／
ｌであり、余剰汚泥発生量は下水処理量１ｍ３あたり
０．１１〜０．１４ｋｇ５ｓ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
とが確認された。Comparative Example Same conditions as in the flow of the present invention shown in Figure 1 except that the sludge solubilization tank and the addition of sulfuric acid were omitted (sewage treatment amount, inflow sewage water quality, aeration tank residence time, and BUD-3S load were the same) As a result of conducting these tests in parallel for the same period, the SVI of activated sludge slurry (7) flowing into the settling tank was 180 to 270,
BOD12~20.5S28~35mg/of sedimentation effluent water
1, and the amount of surplus sludge generated is per 1 m3 of sewage treatment volume.
It was 0.11-0.14 kg5s. This value was about 3 to 4 times larger than that of the present invention, and it was confirmed that the present invention has a large effect.
本発明によれば、次のような効果が得られた。 According to the present invention, the following effects were obtained.
ａ、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。a. With simple operation and equipment, the amount of surplus sludge generated can be significantly reduced. 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.
、ｂ、沈殿槽に流入する活性汚泥の沈降性が、向上する
。, b. The settling properties of the activated sludge flowing into the settling tank are improved.
第１図は、・本発明の処理方法を示す工程図、第２図は
、ｐＨと汚泥の可溶化率の関係を示すグラフ、第３図は
温度と汚泥の可溶化率の関係を示すグラフである。
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・・・鉱酸、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Figure 1 is a process diagram showing the treatment method of the present invention, Figure 2 is a graph showing the relationship between pH and sludge solubilization rate, and Figure 3 is a graph showing the relationship between temperature and sludge solubilization rate. It is. 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... Mineral acid, 13... Concentration process separated water, 14... Solubilized sludge Patent applicant Ebara Infilco Co., Ltd. Ebara Research Institute, Ltd.
Claims (1)
、該固液分離された汚泥の一部を前記好気性生物処理工
程に返送する一方、汚泥の他部に鉱酸を添加し、ｐＨ２
．５以下に維持し、温度５０℃以上の条件で滞留せしめ
て、汚泥中の有機物を可溶化したのち、前記好気性生物
処理工程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 aerobic biological treatment process, while mineral acid is added to the other part of the sludge. , pH2
．． 5 or less and allowing the sludge to remain at a temperature of 50° C. or higher to solubilize organic matter in the sludge, and then supplying the sludge to the aerobic biological treatment step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1095423A JPH02277597A (en) | 1989-04-17 | 1989-04-17 | Treatment of organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1095423A JPH02277597A (en) | 1989-04-17 | 1989-04-17 | Treatment of organic sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02277597A true JPH02277597A (en) | 1990-11-14 |
| JPH0561994B2 JPH0561994B2 (en) | 1993-09-07 |
Family
ID=14137288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1095423A Granted JPH02277597A (en) | 1989-04-17 | 1989-04-17 | Treatment of organic sewage |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02277597A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002035782A (en) * | 2000-07-26 | 2002-02-05 | Japan Organo Co Ltd | Sludge treatment apparatus |
| JP2002361278A (en) * | 2001-06-12 | 2002-12-17 | Hitachi Kiden Kogyo Ltd | Method for removing phosphorus in sludge |
| JP2005334886A (en) * | 2005-08-23 | 2005-12-08 | Kobelco Eco-Solutions Co Ltd | Activated sludge treatment method and activated sludge treatment apparatus therefor |
| JP2010089023A (en) * | 2008-10-09 | 2010-04-22 | Suiwa:Kk | Method for volume-reducing waste sludge |
| CN102718316A (en) * | 2012-06-01 | 2012-10-10 | 天津大学 | Biological denitrification promotion method using carbon source supplemented by carrying out low-intensity ultrasonic sludge disintegration and hydrolytic acidification on disintegrated sludge and straws and application of method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4911813A (en) * | 1972-04-12 | 1974-02-01 | ||
| JPS5157955A (en) * | 1974-11-15 | 1976-05-20 | Eisai Co Ltd | Yojoodeino shorihoho |
| JPS5719719A (en) * | 1980-07-10 | 1982-02-02 | Canon Inc | Electric power source holding device of camera |
-
1989
- 1989-04-17 JP JP1095423A patent/JPH02277597A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4911813A (en) * | 1972-04-12 | 1974-02-01 | ||
| JPS5157955A (en) * | 1974-11-15 | 1976-05-20 | Eisai Co Ltd | Yojoodeino shorihoho |
| JPS5719719A (en) * | 1980-07-10 | 1982-02-02 | Canon Inc | Electric power source holding device of camera |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002035782A (en) * | 2000-07-26 | 2002-02-05 | Japan Organo Co Ltd | Sludge treatment apparatus |
| JP4608057B2 (en) * | 2000-07-26 | 2011-01-05 | オルガノ株式会社 | Sludge treatment apparatus and sludge treatment method |
| JP2002361278A (en) * | 2001-06-12 | 2002-12-17 | Hitachi Kiden Kogyo Ltd | Method for removing phosphorus in sludge |
| JP2005334886A (en) * | 2005-08-23 | 2005-12-08 | Kobelco Eco-Solutions Co Ltd | Activated sludge treatment method and activated sludge treatment apparatus therefor |
| JP2010089023A (en) * | 2008-10-09 | 2010-04-22 | Suiwa:Kk | Method for volume-reducing waste sludge |
| CN102718316A (en) * | 2012-06-01 | 2012-10-10 | 天津大学 | Biological denitrification promotion method using carbon source supplemented by carrying out low-intensity ultrasonic sludge disintegration and hydrolytic acidification on disintegrated sludge and straws and application of method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0561994B2 (en) | 1993-09-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100191219B1 (en) | An efficient treatment of waste water from silicon wafer manufacturing factory | |
| US4341632A (en) | Destruction of bulking sludge | |
| JPH02277597A (en) | Treatment of organic sewage | |
| KR20040078145A (en) | Method and plant for biological treatment of aqueous effluents for purification thereof | |
| JPH0661550B2 (en) | Organic wastewater treatment method | |
| EP0941970A1 (en) | Treatment of aqueous effluents by injection of carbon dioxide | |
| JPH02293095A (en) | Treatment of organic sewage | |
| JP3700938B2 (en) | Method and apparatus for treating combined sewage in rainy weather | |
| JPS6320600B2 (en) | ||
| JP2655284B2 (en) | Treatment method of human wastewater | |
| FI90856B (en) | Process for purification of wastewater or other unclean water and precipitation adjuvant for use in the process | |
| JPH07171600A (en) | Washing concentration of digested sludge and washing concentration agent | |
| JPH03157196A (en) | Treatment of organic sewage | |
| KR0123211B1 (en) | High speed sedimentation method of sludge | |
| US3480541A (en) | Sewage flocculation | |
| JP2001179284A (en) | Method for dephosphorizing excretion wastewater | |
| JPH0230320B2 (en) | ||
| JPS58104696A (en) | Treatment of waste water | |
| JPH0483596A (en) | Treatment of organic sewage | |
| JPH01168399A (en) | Sludge treatment | |
| JPS5919759B2 (en) | Advanced treatment method for sewage water | |
| KR910004128B1 (en) | Concentrated organic waste water treating method | |
| JPH038496A (en) | Treatment of septic tank sludge | |
| Jennett et al. | Treatability of Reverse Osmosis Raffinates by Activated Sludge | |
| SU998383A1 (en) | Apparatus for biologically purifying effluents |