JPH01274899A - Treatment of organic filthy water - Google Patents
Treatment of organic filthy waterInfo
- Publication number
- JPH01274899A JPH01274899A JP63101260A JP10126088A JPH01274899A JP H01274899 A JPH01274899 A JP H01274899A JP 63101260 A JP63101260 A JP 63101260A JP 10126088 A JP10126088 A JP 10126088A JP H01274899 A JPH01274899 A JP H01274899A
- Authority
- JP
- Japan
- Prior art keywords
- water
- sludge
- separated
- membrane
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 239000010802 sludge Substances 0.000 claims abstract description 49
- 239000012528 membrane Substances 0.000 claims abstract description 37
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000002351 wastewater Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 239000007787 solid Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 28
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 230000001112 coagulating effect Effects 0.000 claims 1
- 238000005189 flocculation Methods 0.000 claims 1
- 230000016615 flocculation Effects 0.000 claims 1
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 5
- 239000006228 supernatant Substances 0.000 abstract description 5
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 3
- 239000003002 pH adjusting agent Substances 0.000 abstract description 2
- 239000000654 additive Substances 0.000 abstract 1
- 230000000996 additive effect Effects 0.000 abstract 1
- 238000005345 coagulation Methods 0.000 abstract 1
- 230000015271 coagulation Effects 0.000 abstract 1
- 238000009434 installation Methods 0.000 abstract 1
- 239000012466 permeate Substances 0.000 abstract 1
- 239000010797 grey water Substances 0.000 description 14
- 239000010800 human waste Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000005273 aeration Methods 0.000 description 5
- 230000004907 flux Effects 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 239000004912 1,5-cyclooctadiene Substances 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 229920006317 cationic polymer Polymers 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、し尿、下水、ごみ埋立滲出汚水、各種産業排
水などの有機性汚水の生物学的処理方法に関し、特に生
物学的硝化脱窒素処理と膜分離操作を適用した処理シス
テムの改良に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a biological treatment method for organic wastewater such as human waste, sewage, wastewater from landfills, and various industrial wastewater, and in particular to biological treatment of organic wastewater such as human waste, sewage, wastewater from landfills, and various industrial wastewater. This paper relates to improvements in treatment systems that apply treatment and membrane separation operations.
有機性汚水として最も代表的なし尿を例にあげて説明す
れば、従来のし尿の生物学的処理法として最も進歩した
ものと考えられている方法は、生物学的硝化脱窒素処理
と限外が過（ＵＦ）Ｗｉによる固液分離とを組み合わせ
た処理システムである。Taking human waste, which is the most typical type of organic wastewater, as an example, the most advanced conventional biological treatment methods for human waste are biological nitrification and denitrification and ultraviolet treatment. This is a processing system that combines solid-liquid separation using UF Wi.
このシステムとしては、し尿を生物学的に硝化脱窒素し
、得られた活性汚泥スラリをＵＦ膜で膜分離し、該膜透
過水にＦｅＣ１５＋ ａｌｃｖなどの無Ｒ′ａ集剤を添
加し、残留するＣＯＤ、色度、リンを凝集し、この凝集
フロックをさらにＵＦ膜により膜分離するという方式が
あった（以下、この方式を便宜上、膜分離方式と呼ぶ）
。In this system, human waste is biologically nitrified and denitrified, the resulting activated sludge slurry is membrane-separated using a UF membrane, and a R'a-free collector such as FeC15+ alcv is added to the membrane-permeated water to remove residual There is a method in which COD, chromaticity, and phosphorus are aggregated, and the aggregated flocs are further membrane-separated using a UF membrane (hereinafter, for convenience, this method is referred to as the membrane separation method).
.
このような膜分離方式は、固液分離が確実かつ完璧であ
り、運転管理も容易である上いう、極めて大きな長所が
あるために、当業界において注目を集めている。Such a membrane separation system is attracting attention in the industry because it has extremely great advantages such as reliable and perfect solid-liquid separation and easy operation management.
しかしながら、前記従来の膜分離方式でも、トータルシ
ステムの合理性の立場から評価すると、次のような重大
な問題点が残されていた。However, even in the conventional membrane separation method, when evaluated from the standpoint of the rationality of the total system, the following serious problems remain.
すなわら、膜分離方式による処理システムは、汚泥の脱
水工程から排出される脱水分離水およびし尿搬入東その
他の洗浄排水などの当該処理設備において排出された雑
排水を、し尿と共に生物学的硝化脱窒製工程に流入させ
て処理するため、活性汚泥の分離工程に流入する水量が
増加する（し尿処理量をＱｎ（／日とすると、雑排水蟹
は０．５〜０．８Ｑｄ／日となり、かなりの水量増加を
もたらす）ため、［、Ｊ Ｆ膜による固液骨な工程の設
備コストやランニングコストの大幅な増加を引き起こす
やこのように、従来の膜分離方式は、雑排水の処理を含
めたトータルシステムの合理性において本質的な欠点が
あった、
本発明は、雑排水をも合理的に処理し、固液分離工程の
設備コスト、ランニングコストを節減し得る新規プロセ
スを提供することを目的とするものである。In other words, a membrane separation treatment system processes the dehydrated separated water discharged from the sludge dewatering process and gray water discharged from the treatment facility, such as human waste delivery east and other washing wastewater, along with human waste through biological nitrification. Since the water flows into the denitrification process for treatment, the amount of water flowing into the activated sludge separation process increases (assuming the amount of human waste treated is Qn (/day), gray water crab is 0.5 to 0.8 Qd/day. , resulting in a considerable increase in the amount of water), which causes a significant increase in equipment costs and running costs for solid-liquid processes using JF membranes.In this way, conventional membrane separation methods are difficult to treat gray water. However, the present invention provides a new process that can rationally treat gray water and reduce the equipment cost and running cost of the solid-liquid separation process. The purpose is to
〔課題を解決するだめの手段〕
本発明は、有機性汚水を生物学的硝化脱窒素処理したの
ち、活性汚泥を固液分離し、分離された生物処理水に無
機凝集剤を添加して凝集７膜分離する一方、分離された
活性汚泥の余剰分を当該処理設・備において排出された
雑排水と共に嫌気及び好気処理したのち脱水し７、該脱
水分離水を前記生物処理水と共に凝集、膜分離すること
を特徴とする有機性汚水の処理方法である。[Means for Solving the Problems] The present invention performs biological nitrification and denitrification treatment on organic wastewater, separates activated sludge into solid and liquid, and adds an inorganic flocculant to the separated biologically treated water to flocculate it. 7 While performing membrane separation, the surplus of the separated activated sludge is subjected to anaerobic and aerobic treatment along with gray water discharged in the treatment equipment/equipment, and then dehydrated 7, and the dehydrated separated water is coagulated with the biologically treated water, This is a method for treating organic wastewater characterized by membrane separation.
本発明の作用を、し尿処理を例にとりあげ、−実施態様
を示す第１図を参照しながら詳しく説明する。The operation of the present invention will be explained in detail by taking human waste treatment as an example, with reference to FIG. 1 which shows an embodiment.
除渣し尿ｌは、生物学的硝化脱窒製工程２（公知の回分
型、硝化液循環型などを適用すればよい）に導かれ、Ｂ
ＯＤ、窒素成分などが除去されたのち１、二の活性汚泥
スラリ３がｉＪ Ｆ膜または遠心分離等による固液分離
工程４に流入し、生物処理水５と濃縮汚泥６とに分離さ
れ、生物処理水５は生物処理水貯槽７に貯留される。The removed human waste l is led to biological nitrification and denitrification process 2 (a known batch type, nitrification liquid circulation type, etc. may be applied), and B
After OD, nitrogen components, etc. have been removed, the activated sludge slurries 1 and 2 flow into a solid-liquid separation process 4 using an iJF membrane or centrifugation, where they are separated into biologically treated water 5 and thickened sludge 6. The treated water 5 is stored in a biologically treated water storage tank 7.
固液分離工程４で分離された濃縮汚泥６の大部分は返送
汚泥８と・して、生物学的硝化脱窒製工程２にリサイク
ルされ、残部は余剰汚泥９として、当該処理設備におい
て排出されたし尿搬入車洗浄排水、各種洗浄排水などの
雑排水１０と共に、嫌気・好気生物処理工程１１に供給
され、散気装置１２による曝気の０Ｎ−ＯＦＦを繰り返
す回分型の嫌気・好気処理、または通常の嫌気処理と好
気処理により、雑排水１０中のＢＯＤ、 ＣＯＤ、窒素
、リンなどを生物学的に除去したのち、該工程において
汚泥を沈降させ、この沈降ｔη泥１３にポリマなどの脱
水助剤１４を添加し、汚泥脱水機１５ （遠心脱水機、
ベルトプレスなど）に供給する。Most of the concentrated sludge 6 separated in the solid-liquid separation step 4 is recycled to the biological nitrification and denitrification step 2 as return sludge 8, and the remainder is discharged as surplus sludge 9 in the treatment facility. Batch-type anaerobic/aerobic treatment is supplied to an anaerobic/aerobic biological treatment process 11 together with gray water 10 such as human waste truck washing wastewater and various washing wastewater, and aeration is repeatedly turned on and off by an aeration device 12. Or, after biologically removing BOD, COD, nitrogen, phosphorus, etc. in the gray water 10 by normal anaerobic treatment and aerobic treatment, the sludge is sedimented in this process, and polymers etc. are added to this sedimented tη mud 13. A dewatering aid 14 is added to the sludge dewatering machine 15 (centrifugal dewatering machine,
belt press, etc.).
一方、嫌気・好気生物処理工程＋１からの上澄水１６と
汚泥脱水［１５の脱水分離水１７の両者を生物処理水貯
槽７に供給し、生物学的硝化脱窒素された生物処理水５
と混合する。On the other hand, both the supernatant water 16 from the anaerobic/aerobic biological treatment process +1 and the dehydrated separated water 17 from the sludge dehydration [15] are supplied to the biologically treated water storage tank 7, and the biologically treated water 5 is subjected to biological nitrification and denitrification.
Mix with.
しかして、生物処理水貯槽７の混合液に対して、無機凝
集剤１８ （ＦｅＣ１ｓ、ポリ硫酸鉄などのＦｅ”塩が
最も好ましい）と、ｐｎ調整剤（ＮａＯＨなど）１９を
添加し、混和して凝集フロックを形成させたのち、ＵＦ
膜、精密が過（ＭＦ）膜などの膜分離工程２０により凝
集フロックを分離し、完全に清澄な膜透過水２１を取り
出す。この膜透過水２１は、所望により活性炭吸着処理
される。Therefore, an inorganic flocculant 18 (most preferably Fe" salts such as FeCls and polyferric sulfate) and a pn adjuster (NaOH, etc.) 19 are added to the mixed liquid in the biologically treated water storage tank 7 and mixed. After forming agglomerated flocs, UF
The aggregated flocs are separated by a membrane separation step 20 such as a membrane or MF membrane, and completely clear membrane permeated water 21 is taken out. This membrane-permeated water 21 is subjected to activated carbon adsorption treatment, if desired.
なお、膜分離工程２０で分離されたスラッジ２２中の水
分の水質は、すでに汚濁成分が除去されているので、嫌
気・好気生物処理工程１１に流入させる必要なく、脱水
助剤１４を添加したのち、直接汚泥脱水機１５に供給し
てよい。In addition, since the water quality of the water in the sludge 22 separated in the membrane separation step 20 has already removed pollutant components, the dehydration aid 14 is added without the need to flow it into the anaerobic/aerobic biological treatment step 11. Afterwards, it may be directly supplied to the sludge dewatering machine 15.
本発明の実施例として第１図に示すフローに従い、表−
１に示す除渣し尿を、公知の硝化液循環型の生物学的硝
化脱窒製工程（第１脱窒素槽−硝化槽一第２脱窒素槽−
再曝気槽を直列配置したもの）に供給し、表−２に示す
運転条件で処理した。As an embodiment of the present invention, according to the flow shown in FIG.
The desalted human waste shown in 1 was processed in a known nitrifying solution circulation type biological nitrification and denitrification process (first denitrification tank - nitrification tank - second denitrification tank -
reaeration tanks arranged in series) and processed under the operating conditions shown in Table 2.
以下余白
表−１除渣し２尿水質
表−２生物学的硝化脱窒製工程の運転条件法に、生物学
的硝化脱窒製工程より流出する活性汚泥を、分画分子量
ｌＯ万（公称値）のチューブラ−型ＩＰ膜でクロスフロ
ーにより膜分離した。ｔｌＦ膜透過流束（フラックス）
は１．４ｆｆｌ／耐・膜・日とい・う高い値が安定して
得られ、膜透過水の水質は表−３のとおりであった。The activated sludge discharged from the biological nitrification and denitrification process was calculated using the following margin table - 1 Slag removal and 2 Urine water quality table - 2 Operating conditions for the biological nitrification and denitrification process. Membrane separation was carried out by cross-flow using a tubular type IP membrane of tlF membrane permeation flux (flux)
A high value of 1.4 ffl/membrane day was stably obtained, and the quality of the membrane permeated water was as shown in Table 3.
表−３
一方、し原産入車洗浄排水などの当該処理設備で排出さ
れた雑排水（ＳＳ ５００〜１２００■／ｇ、ＢＯＤ８
００〜９５０■／Ｌ Ｔ−Ｎ ２５０〜２７５■／ｌ＞
に、前記ＵＦ膜分離工程で分離された汚泥のうち余剰活
性汚泥相当分を添加し、回分型活性汚泥法により、雑排
水の汚濁成分を処理した９回分型活性汚泥法の操作条件
は、汚水流入０．５時間−曝気を２０分、曝気停止を１
０分のサイクルを３時間繰り返す一曝気停止活性汚泥沈
殿１時間−上澄水抜き出し０．５時間というシーケンス
に設定して行った。その回分槽の活性汚泥の１’ＩＬＳ
Ｓは２５００〜３０００■／Ｉ！となった。また、沈殿
汚泥にカチオンポリマ（荏原インフィルコ■商品名 エ
バグロース１０４Ｇ）を１．５％ｔｏ ５５添加して凝
集フロック形成させたのち、デカンタ型遠心脱水機で脱
水して得た脱水分離水と、前記の回分型活性汚泥処理の
上澄水とを、前記生物学的硝化脱窒素工程−〇Ｆ膜分離
工程からの膜透過水槽に流入させ、エアー攪拌した混合
液の水質は表−４のようであった。Table 3 On the other hand, gray water (SS 500-1200/g, BOD8
00~950■/L T-N 250~275■/L>
The operating conditions for the 9-batch activated sludge method were as follows: Adding an equivalent amount of surplus activated sludge from the sludge separated in the UF membrane separation step to the 9-batch activated sludge method to treat the pollutant components of gray water. , sewage inflow 0.5 hours - aeration for 20 minutes, aeration stop for 1 hour
The sequence was set such that a cycle of 0 minutes was repeated for 3 hours, aeration was stopped, activated sludge sedimentation was performed for 1 hour, and supernatant water was removed for 0.5 hours. 1'ILS of activated sludge in the batch tank
S is 2500~3000■/I! It became. In addition, 1.5% to 55 of a cationic polymer (Ebara Infilco's trade name Evagrowth 104G) was added to the precipitated sludge to form coagulated flocs, and then the dehydrated separated water obtained by dehydrating with a decanter-type centrifugal dehydrator and the above-mentioned The supernatant water from the batch-type activated sludge treatment was flowed into the membrane permeation water tank from the biological nitrification and denitrification process - 〇F membrane separation process, and the water quality of the mixed liquid after air stirring was as shown in Table 4. there were.
表−４
次に、皮−４の水質を示す混合液に対し、ＦｅＣｌ５を
２００（ｈｒ ／ ｌ添加し、ＮａＯＨでｐＨ４，５〜
５．０に中和してフロック形成せしめた後、分画分子ｆ
ｆ１ｌＯ万のチエ−プラー型ＵＦ膜モジュールにより、
モジュール内流速２．２ ｍ ／ ｓｅｅでクロスフロ
ーフィルトレージタンした結果、膜透過流束ば２． Ｏ
ｒｄ ／ ｒｄ・膜・日と、前記の活性汚泥のＵＦ膜分
離工程のフラックスよりもかなり大きな値が安定して得
られた。Table 4 Next, 200 (hr/l) of FeCl5 was added to the mixed solution showing the water quality of Peel-4, and the pH was adjusted to 4.5-5 with NaOH.
After neutralizing to 5.0 to form flocs, the fractionated molecule f
With f110 million Cheapler type UF membrane module,
As a result of cross-flow filtration at a flow rate of 2.2 m/see in the module, the membrane permeation flux was 2. O
A value of rd/rd/membrane/day, which is considerably larger than the flux of the activated sludge UF membrane separation process described above, was stably obtained.
ＵＦ膜透過水の水質は表−５の如く極めて高度のもので
あった。The quality of the water permeated through the UF membrane was extremely high as shown in Table 5.
表−５
〔発明の効果〕
以十述べたようｔご本発明によれば、次のような多くの
効果を得ることができ、従来方式の課題を解決すること
ができる。Table 5 [Effects of the Invention] As described above, according to the present invention, many of the following effects can be obtained and the problems of the conventional system can be solved.
■ 排水量が多い雑排水を、有機性汚水の生物学的膜窒
素工程に流入させることなく、別個に設けられた嫌気及
び好気処理工程に供給して処理するので、生物学的硝化
脱窒製工程に後続する活性汚泥の固液分離工程への流入
水量が、従来方式に比べて大幅に減少する。その結果、
活性汚泥の固液分離工程の設備コストおよびランニング
コストが減少され、ユーザのコスト負担が軽減され、省
エネルギーも実現できる。■ A biological nitrification and denitrification system is used to treat gray water, which has a large amount of wastewater, by supplying it to separate anaerobic and aerobic treatment processes without flowing it into the organic wastewater biological membrane nitrogen process. The amount of water flowing into the activated sludge solid-liquid separation process that follows the process is significantly reduced compared to conventional methods. the result,
The equipment cost and running cost of the solid-liquid separation process of activated sludge are reduced, the cost burden on the user is reduced, and energy savings can also be realized.
■ 水温が低く排水量が多い雑排水が有機性汚水の生物
学的硝化脱窒製工程に流入しないので、生物学的硝化脱
窒製工程の水温を、硝化、脱窒菌にとって好適な３５〜
４０℃に維持しやすく、効率的な生物処理を行うことが
できる。■ Since gray water with a low water temperature and a large amount of wastewater does not flow into the biological nitrification and denitrification process of organic wastewater, the water temperature in the biological nitrification and denitrification process has been adjusted to a temperature of 35 to 35°C, which is suitable for nitrification and denitrification bacteria.
It is easy to maintain the temperature at 40°C, and efficient biological treatment can be performed.
■ 従来方式では、生物学的硝化脱窒製工程の余剰汚泥
が脱水する前に汚泥貯留槽で滞留している間に、嫌員的
になって汚泥からＮＨ３−Ｎが溶出し、これを除去する
ための前記生物学的硝化脱窒製工程の窒素負荷を高める
という問題点があったが、本発明では余剰汚泥を雑排水
と混合し、余剰汚泥中の微生物を利用しχ雑排水中の汚
濁成分を除去しつつ、微生物の活性を維持するんで、前
記従来の間Ｂ（汚泥からのＮｌ！、−Ｎの溶出）が発生
しない。■ In the conventional method, while the surplus sludge from the biological nitrification and denitrification process remains in the sludge storage tank before being dehydrated, NH3-N is eluted from the sludge and removed. However, in the present invention, surplus sludge is mixed with gray water and microorganisms in the surplus sludge are used to reduce the amount of nitrogen in the gray water. Since the activity of microorganisms is maintained while removing pollutant components, B (elution of Nl!, -N from sludge) does not occur as in the conventional method.
第１図は本発明の一実施態様を示すフローシートである
。
１・・・除渣し尿、２・・・生物学的硝化脱窒製工程、
３・・・活性汚泥スラリ、４・・・固液分離工程、５・
・・生物処理水、６・・・濃縮汚泥、７・・・生物処理
水貯槽、８・・・返送汚泥、９・・・余剰汚泥、１０・
・・雑排水、１１・・・嫌気・好気生物処理工程、１２
・・・散気装置、１３・・・沈降汚泥、１４・・・脱水
助剤、１５・・・汚泥脱水機、１６・・・上澄水、１７
・・・脱水分離水、１８・・・、無機凝集剤、１９・・
・ｐＨ調整剤、２０・・・膜分離工程、２１・・・膜透
過水、２２・−・スラッジ。FIG. 1 is a flow sheet showing one embodiment of the present invention. 1... Sludge removal human waste, 2... Biological nitrification and denitrification process,
3...Activated sludge slurry, 4...Solid-liquid separation process, 5.
... Biologically treated water, 6... Thickened sludge, 7... Biologically treated water storage tank, 8... Returned sludge, 9... Excess sludge, 10.
... Gray water, 11 ... Anaerobic/aerobic biological treatment process, 12
... air diffuser, 13 ... settled sludge, 14 ... dewatering aid, 15 ... sludge dehydrator, 16 ... supernatant water, 17
...Dehydrated separated water, 18..., Inorganic flocculant, 19...
- pH adjuster, 20... Membrane separation step, 21... Membrane permeation water, 22... Sludge.
Claims (1)
活性汚泥を固液分離し、分離された生物処理水に無機凝
集剤を添加して凝集、膜分離する一方、分離された活性
汚泥の余剰分を当該処理設備において排出された雑排水
と共に嫌気及び好気処理したのち脱水し、該脱水分離水
を前記生物処理水と共に凝集、膜分離することを特徴と
する有機性汚水の処理方法。(1) After biological nitrification and denitrification treatment of organic wastewater,
Activated sludge is separated into solid and liquid, and an inorganic flocculant is added to the separated biologically treated water for flocculation and membrane separation. 1. A method for treating organic wastewater, which comprises performing aerobic treatment, dehydration, and coagulating and membrane-separating the dehydrated separated water together with the biologically treated water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63101260A JPH0649196B2 (en) | 1988-04-26 | 1988-04-26 | Organic wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63101260A JPH0649196B2 (en) | 1988-04-26 | 1988-04-26 | Organic wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01274899A true JPH01274899A (en) | 1989-11-02 |
| JPH0649196B2 JPH0649196B2 (en) | 1994-06-29 |
Family
ID=14295945
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63101260A Expired - Lifetime JPH0649196B2 (en) | 1988-04-26 | 1988-04-26 | Organic wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0649196B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100397168B1 (en) * | 2001-02-02 | 2003-09-06 | (주)범한엔지니어링 종합건축사 사무소 | Apparatus and Method For Animal Waste water Treatment |
| WO2005061398A1 (en) * | 2003-12-24 | 2005-07-07 | Bushwater Holdings Pty Ltd | A system for water treatment |
| JP2006061743A (en) * | 2004-08-24 | 2006-03-09 | Asahi Kasei Clean Chemical Co Ltd | Method and apparatus for treating excess sludge |
-
1988
- 1988-04-26 JP JP63101260A patent/JPH0649196B2/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100397168B1 (en) * | 2001-02-02 | 2003-09-06 | (주)범한엔지니어링 종합건축사 사무소 | Apparatus and Method For Animal Waste water Treatment |
| WO2005061398A1 (en) * | 2003-12-24 | 2005-07-07 | Bushwater Holdings Pty Ltd | A system for water treatment |
| JP2006061743A (en) * | 2004-08-24 | 2006-03-09 | Asahi Kasei Clean Chemical Co Ltd | Method and apparatus for treating excess sludge |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0649196B2 (en) | 1994-06-29 |
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