JPH01293196A - Treatment of organic sewage - Google Patents
Treatment of organic sewageInfo
- Publication number
- JPH01293196A JPH01293196A JP63123920A JP12392088A JPH01293196A JP H01293196 A JPH01293196 A JP H01293196A JP 63123920 A JP63123920 A JP 63123920A JP 12392088 A JP12392088 A JP 12392088A JP H01293196 A JPH01293196 A JP H01293196A
- Authority
- JP
- Japan
- Prior art keywords
- sewage
- separated
- slurry
- membrane
- flocculant
- 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 12
- 239000012528 membrane Substances 0.000 claims abstract description 30
- 239000002002 slurry Substances 0.000 claims abstract description 20
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 11
- 229920000642 polymer Polymers 0.000 claims abstract description 6
- 238000000034 method Methods 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 21
- 239000011777 magnesium Substances 0.000 claims description 9
- 239000002351 wastewater Substances 0.000 claims description 9
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 8
- 229910052749 magnesium Inorganic materials 0.000 claims description 8
- 238000005189 flocculation Methods 0.000 claims description 6
- 230000016615 flocculation Effects 0.000 claims description 4
- 230000000813 microbial effect Effects 0.000 claims description 2
- 239000010802 sludge Substances 0.000 abstract description 23
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 4
- 239000002245 particle Substances 0.000 abstract description 4
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 2
- 244000144992 flock Species 0.000 abstract 3
- 239000003513 alkali Substances 0.000 abstract 2
- 230000001546 nitrifying effect Effects 0.000 abstract 2
- 239000010800 human waste Substances 0.000 description 11
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 8
- 238000000108 ultra-filtration Methods 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 229920006317 cationic polymer Polymers 0.000 description 2
- 239000008394 flocculating agent Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 229910015400 FeC13 Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000009527 percussion Methods 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 210000002700 urine Anatomy 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
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、し原糸汚水、下水、ごみ埋立滲出汚水、各種
産業廃水などの有機性汚水を、新規な概念、構成により
合理的に処理し、常に安定して裔度に浄化された処理水
を得る方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention is capable of rationally treating organic sewage such as yarn sewage, sewage, landfill effluent sewage, and various industrial wastewater using a new concept and structure. The present invention also relates to a method for obtaining treated water that is consistently and thoroughly purified.
し尿等の有機性汚水を処理するための最も新しい方式は
、
る。The newest method for treating organic wastewater, such as human waste, is
この膜分離方式は、活性汚泥及び凝集フロックの固液分
離が常に完璧であり、維持管理も容易であるという極め
て重要な長所をもっているため、非常に脚光を浴びてい
る。This membrane separation method has been attracting much attention because it has the extremely important advantages of always perfect solid-liquid separation of activated sludge and coagulated flocs and easy maintenance.
しかしながら、このような新しい膜分離方式でも、次の
ような重大な問題点が未解決であり、さらに優れた処理
プロセスの開発が切望されている。However, even with such a new membrane separation method, the following serious problems remain unsolved, and there is a strong need for the development of an even better treatment process.
すなわち、 ■ 生物学的硝化脱窒素処理水中に残留するＣＯＤ。That is, ■ COD remaining in biological nitrification and denitrification treated water.
色度及びｐｏ、’−を凝集除去するために多量のＦｅＣ
ｌ ３注入率（２０００〜３０００ｗ／ １ ）を必要
とし、必然的にＦｅ（０１１）ｉ、 ＦｅＰＯａを主体
とする難脱水性のＤ集汚泥の発生量が多くなる。この結
果、汚泥処理工程の設備費、運転費が増加する。Large amount of FeC to agglomerate remove chromaticity and po,'-
13 injection rate (2000 to 3000 w/1) is required, which inevitably increases the amount of D-collected sludge, which is difficult to dewater, and is mainly composed of Fe(011)i and FePOa. As a result, equipment costs and operating costs for the sludge treatment process increase.
■ 限外ｔＰ遇膜による固液分離工程を２段階必要とし
ているので、固液分離のための設備費及びランニングコ
ストが高くなる。例えば、限外が過膜分離工程のランニ
ングコストは、２段階を合せて、し尿ｌｋｌあたり５０
０〜６００円という非常に高額となり、ユーザーのコス
ト負担が著しく増大する。(2) Since a two-step solid-liquid separation process using an ultra-tP membrane is required, equipment costs and running costs for solid-liquid separation are high. For example, the running cost of the ultrafiltration membrane separation process is 50 yen per lkl of human waste, including the two stages.
The cost is extremely high, ranging from 0 to 600 yen, and the cost burden on the user increases significantly.
本発明は、このような膜分離方式の重大欠点を完全に解
決することを目的としており、具体的には、
■ 凝集汚泥の発生量を大幅に減少させ、汚泥処理、処
分工程を合理化すること。The purpose of the present invention is to completely solve these serious drawbacks of the membrane separation method, and specifically: (1) significantly reduce the amount of flocculated sludge generated and streamline the sludge treatment and disposal process; .
■ 活性汚泥の固液分離にのみ限外が過膜を適用し、凝
集汚泥の固液分離用の限外ヂ過膜の設置を不要にするこ
と。すなわち、限外濾過膜工程の設備コスト、ランニン
グコストを従来に比べて半減させること。■ Apply ultrafiltration membrane only to solid-liquid separation of activated sludge, making it unnecessary to install ultrafiltration membrane for solid-liquid separation of flocculated sludge. In other words, the equipment cost and running cost of the ultrafiltration membrane process can be halved compared to conventional methods.
■ 従来の膜分離方式では、し尿中のリン酸分をＦｅＰ
Ｏａ汚泥として処分せざるを得す、有効利用することが
できなかったが、リン酸分を肥料として有効利用しやす
い形態で回収する方法を確立すること。■ In the conventional membrane separation method, the phosphoric acid content in human waste is removed using FeP.
Although the phosphoric acid content had to be disposed of as Oa sludge and could not be used effectively, it is necessary to establish a method for recovering the phosphoric acid content in a form that can be easily used effectively as fertilizer.
などを解決課題としている。These are the issues to be solved.
本発明は、有機性汚水にマグネシウム系アルカリ剤と高
分子凝集剤を添加し混和したのち固液分離し、得られた
分離液を生物学的１＋ｌ’ｉ化脱窒素処理工程にて処理
し、該工程内もしくは該工程から流出する微生物スラリ
にＦｅ”系又はへ１３゛系凝集剤を添加して凝集せしめ
、該凝集スラリを膜分離し、分離された７ｒｉ縮スラリ
の一部を前記生物学的硝化脱窒製処理工程へ返送すると
共に、残部を前記有機性汚水に混合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 involves adding and mixing a magnesium-based alkaline agent and a polymer flocculant to organic wastewater, followed by solid-liquid separation, and treating the resulting separated liquid in a biological 1+l'i denitrification treatment process, A Fe''-based or He13''-based flocculant is added to the microbial slurry flowing out of the process or from the process to cause flocculation, the flocculated slurry is separated by a membrane, and a part of the separated 7ri condensed slurry is used as the biological This method of treating organic wastewater is characterized in that the waste water is returned to the target nitrification and denitrification treatment process, and the remainder is mixed with the organic wastewater.
６作 用〕
本発明の一実施態様を示す図面を参照しながら、以下に
本発明の作用を詳しく説明する。6 Effects] The effects of the present invention will be described in detail below with reference to the drawings showing one embodiment of the present invention.
搬入されたし尿ｌに後述する余剰濃縮スラリ２を添加混
合したのち、マグネシウム系アルカリ剤３ （Ｍｇ（Ｏ
ｌｌ）ｔの使用が好適）を加え、さらに高分子凝集剤４
（カチオンポリマが好適）を添加し、混和してフロッ
クを形成したのち、ウェッジワイヤスクリーン５ （目
開き０．５鶴程度の回転式スクリーンの採用が好適）に
よってフロックを分離する。Excess concentrated slurry 2 (described later) is added to and mixed with the carried human waste 1, and then magnesium-based alkaline agent 3 (Mg(O
(It is preferable to use
After adding (preferably a cationic polymer) and mixing to form flocs, the flocs are separated by a wedge wire screen 5 (preferably a rotary screen with an opening of about 0.5 mm).
し尿１に余剰濃縮スラリ２、マグネシウム系アルカリ剤
３及びポリマ４を添加混合することによって生成するフ
ロックの性状は、し尿１中のＰＯ４’−とＮＨ，”が−
ｇ２゛と反応して生成した結晶性Ｎｌ！４ＭｇＰＯｅ粒
子と、し尿ｌ中の繊維分、 ＳＳが一体化した、強度の
大きな脱水性の良好なものとなっており、ウェッジワイ
ヤスクリーン５で分離されたスクリーン分１ｉｉｉ！汚
泥６は、スクリュープレス脱水機、ベルトプレス脱水機
などの機械脱水機７によって効果的に低水分の脱水ケー
キ８ （スクリュープレスを適用する場合は、脱水ケー
キ水分は６５％以下のものが得られる）に変換される。The properties of the floc produced by adding and mixing excess concentrated slurry 2, magnesium-based alkaline agent 3, and polymer 4 to human waste 1 are such that PO4'- and NH,'' in human waste 1 are -
Crystalline Nl produced by reaction with g2゛! 4MgPOe particles, fibers in human waste 1, and SS are integrated into a product with great strength and good dehydration properties, and the screen portion separated by wedge wire screen 5 is 1iii! The sludge 6 is effectively reduced to a low-moisture dehydrated cake 8 by a mechanical dehydrator 7 such as a screw press dehydrator or a belt press dehydrator (if a screw press is used, a dehydrated cake with a moisture content of 65% or less can be obtained) ) is converted to
この脱水ケーキ８は、低水分で取扱いも楽であり、リン
酸含有量が多く肥料として有効利用することができる。This dehydrated cake 8 has a low moisture content, is easy to handle, and has a high phosphoric acid content, so it can be effectively used as fertilizer.
一方、ウェッジワイヤスクリーン５でｓｓ、 ｓｓ性Ｂ
ＯＤ及びＰ０４′−の大部分（８０〜９０％程度）が除
去されたスクリーン分離液９を、無希釈の生物学的硝化
脱窒製処理工程１０（公知の回分型、硝化液循環型を適
用すればよい）に供給して硝化脱窒素処理を行い、スク
リーン分離液中の窒素成分。On the other hand, with wedge wire screen 5, ss, ss property B
The screen separated liquid 9 from which most of the OD and P04'- (approximately 80 to 90%) have been removed is subjected to an undiluted biological nitrification and denitrification treatment step 10 (a known batch type or nitrification liquid circulation type). Nitrogen components in the screen separated liquid are supplied to a nitrification and denitrification process.
ＢＯＤ成分などを生物学的に除去する。この過程におい
て、スクリーン分離液９中に少量残留しているＰＯ４’
−も、活性汚泥に摂取されて除去される。Biologically removes BOD components etc. In this process, a small amount of PO4' remains in the screen separation liquid 9.
- is also taken up by the activated sludge and removed.
次に、生物学的硝化脱窒製処理工程１０から流出する活
性汚泥スラリ１１に、ｐ ｅ ３ ＊系又はＡＩ”系凝
集剤１２ （ＦｅＣ１，もしくはポリ硫酸第２鉄、＾ｌ
ｕｍ。Next, the activated sludge slurry 11 flowing out from the biological nitrification and denitrification treatment process 10 is treated with a p e 3 *-based or AI"-based flocculant 12 (FeC1, or polyferric sulfate,
um.
ＰＡＣの使用が好適）を添加して、活性汚泥スラリｌｌ
中に含まれる非生物分解性ＣＯＤ成分及びコロイド状粒
子成分を凝集せしめたのち、限外が過膜。PAC) is added to the activated sludge slurry.
After coagulating the non-biodegradable COD components and colloidal particle components contained therein, ultrafiltration is performed.
精密濾過膜などを装着した膜モジュール１３（分画分子
量４〜１０万程度のチューブラ又は平膜タイプの限外Ｆ
ｉモジュールの適用が好ましい）に供給して完璧に固液
分離し、ＳＳゼロの全く清澄な膜ｉ３過水１４と濃縮ス
ラリ１５に分離する。Membrane module 13 equipped with a precision filtration membrane, etc. (tubular or flat membrane type ultra-F with a molecular weight cut-off of about 40,000 to 100,000)
i module is preferably applied) for complete solid-liquid separation and separation into completely clear membrane i3 with zero SS 14 and concentrated slurry 15.
膜モジュール１３によって分離された濃縮スラリ１５の
大部分は、生物学的硝化脱窒素処理工程１０にリサイク
ルされるが、残部の余剰分たる余刺淵縮スラリ２を前述
のようにし尿１に混合し、し尿中のＳＳ等と共に凝集せ
しめるようにする。Most of the concentrated slurry 15 separated by the membrane module 13 is recycled to the biological nitrification and denitrification treatment step 10, but the remaining surplus slurry 2 is mixed with human waste 1 as described above. It is made to aggregate with SS etc. in human urine.
以上の実施態様で述べたように、本発明の技術思想の骨
子は、
（イ）打機性汚水と膜分離された余剰濃縮スラリとの混
合液に、マグネシウム系アルカリ剤とポリマとを添加し
、凝集フロック及びＮＩＩ４ＭｇＰＯ，粒子を固液分離
する点
（訂）このような前処理を受けてＰＯ，’−濃度とＳＳ
が大幅に減少した液を生物学的硝化脱窒素処理したのち
、Ｆｅ ５ ＋系又はＡ１３゛系凝集剤によって凝集処
理し、膜分離する点
という２つの技術を結合させた思想に要約される。As described in the above embodiments, the gist of the technical idea of the present invention is as follows: (a) A magnesium-based alkaline agent and a polymer are added to the mixed liquid of percussion wastewater and membrane-separated excess concentrated slurry. , solid-liquid separation of flocs and NII4MgPO, particles (edited) After undergoing such pretreatment, PO,'-concentration and SS
The idea can be summarized as a combination of two techniques: after biological nitrification and denitrification treatment of a liquid in which the amount of carbon dioxide has been significantly reduced, flocculation treatment is performed using a Fe 5 + type or A13'' type flocculant, and membrane separation is performed.
滋賀県ｌ郡衛生プラントに搬入されたし尿に、後述する
限外濾過膜を装着したチューブラ型膜モジュールで分離
された濃縮活性汚泥の余剰分を混合し、Ｍｇ （Ｏｆｆ
） ｚを１０００■／β添加して２〜３分攪拌したのち
、カチオンポリマとしてエバグロースＣ１０４Ｇ（荏原
インフィルコ■商品名〕を２００〜２５０１Ｗ／ｊ！添
加したところ、巨大なフロックが速やかに形成された。Excess concentrated activated sludge separated by a tubular membrane module equipped with an ultrafiltration membrane (described later) is mixed with human waste brought to the Sanitation Plant in District I, Shiga Prefecture.
) was added at 1000■/β and stirred for 2 to 3 minutes, and then 200 to 2501W/J! of Evagrowth C104G (trade name of Ebara Infilco) was added as a cationic polymer, and huge flocs were quickly formed. .
しかるのち、目開き０．５１■の回転式ウェッジワイヤ
スクリーンに供給したところ、容易にフロックは分離さ
れ、表−１の水質を示すスクリーン分離液が得られた。Thereafter, when the water was fed to a rotating wedge wire screen with a mesh size of 0.51 square meters, the flocs were easily separated, and a screen-separated liquid having the water quality shown in Table 1 was obtained.
表−１
このスクリーン分離液を公知の硝化液循環型生物学的硝
化脱窒製処理工程で無希釈処理した。この時の運転条件
は、表−２のように設定した。Table 1 This screen separated liquid was treated without dilution using a known nitrification liquid circulation type biological nitrification and denitrification treatment process. The operating conditions at this time were set as shown in Table-2.
表−２
次に、この生物学的硝化脱窒素処理工程の最終段の再曝
気槽から流出する活性汚泥スラリに対し、ＦｅＣ１３を
１６００＋ｗ／ｊ！添加し、Ｎａ０１ｌでｐｌ＋を５．
０〜５．２に調整して２分間撹拌したのち、公称分画分
子量１０万のポリオレフィン製限外ヂ過膜を装着したチ
ューブラ型モジュールに流速１．５ ｍ／ｓｅｃで供給
し、クロスフローフィルトレージョンした。この結果、
限外Ｕｉ過膜の透過流速（Ｆｌｕｘ）は１．４ｎ’ｒ／
イ一膜面積・日となり、膜透過水の水質は、表−３のよ
うに極めて良好であった。Table 2 Next, 1600+w/j of FeC13 was added to the activated sludge slurry flowing out from the reaeration tank at the final stage of this biological nitrification and denitrification treatment process! 5. Add pl+ with Na01l.
After adjusting the temperature to 0 to 5.2 and stirring for 2 minutes, it was supplied at a flow rate of 1.5 m/sec to a tubular module equipped with a polyolefin ultrafiltration membrane with a nominal molecular weight cutoff of 100,000, and the cross-flow filter Trasion was done. As a result,
The permeation flow rate (Flux) of the ultra-Ui membrane is 1.4 n'r/
The water quality of the water permeated through the membrane was extremely good as shown in Table 3.
表−３
一方、この膜分離で分離された濃縮活性汚泥の大部分を
生物学的硝化脱窒素処理工程にリサイクルし、残部の余
剰分を処理されるべきし尿に混合した。Table 3 On the other hand, most of the concentrated activated sludge separated by this membrane separation was recycled to the biological nitrification and denitrification treatment process, and the remaining surplus was mixed with the human waste to be treated.
また、生物学的硝化脱窒素処理工程の前段に設けた前述
の回転式ウェッジワイヤスクリーンから排出された分離
汚泥を、直径３００＋ｕφ、長さ１．５ｍのスクリュー
プレス脱水機で脱水したところ、非常に効果的に脱水さ
れ、水分６３〜６５％のケーキが得られた。In addition, when the separated sludge discharged from the aforementioned rotating wedge wire screen installed at the front stage of the biological nitrification and denitrification process was dewatered using a screw press dehydrator with a diameter of 300+uφ and a length of 1.5 m, it was found that A cake was obtained which was effectively dehydrated and had a moisture content of 63-65%.
■ あらかじめ有機性汚水中のｐｏ、３−の大部分をＮ
ＩＩＪｇＰＯａとして除去したのち、生物学的硝化脱窒
素処理工程でさらにｐｏ、’−を活性汚泥内にとり込ん
で除去するので、その後に添加されるＦｅ”系凝集剤が
ｐｏ、’−の除去のために消費されることなく 、ＣＯ
Ｄ 、色度などの除去に消費される。この結果、ＦｅＣ
ｌ、１などのＦｅｈ系凝集剤の所要量が、前述した従来
の膜分離方式に比較して２７３程度に減少し、汚泥発生
量も減少するから、汚泥の処理、処分工程の合理化がで
きる。■ Most of the po and 3- in organic wastewater are replaced with N in advance.
After removing it as IIJgPOa, po,'- is further incorporated into activated sludge and removed in the biological nitrification and denitrification treatment process, so the Fe''-based flocculant added afterwards is used to remove po,'-. CO without being consumed by
D, consumed for removing chromaticity, etc. As a result, FeC
The required amount of Feh-based flocculants such as 1 and 1 is reduced to about 273 compared to the conventional membrane separation method described above, and the amount of sludge generated is also reduced, so the sludge treatment and disposal process can be streamlined.
■ マグネシウム系アルカリ剤の添加を受けた有機性ｌ
η水を、生物学的硝化脱窒素処理したのちＦｅ”系又は
ＡＩ”系凝集剤を添加して凝集処理するようにした結果
、凝集処理工程でのアルカリ剤が大幅に減少できる。す
なわち、マグネシウム系アルカリ剤が、ｐｏ４″−の除
去と凝集工程用のρ１）調整剤との２つの機能を果たす
。■ Organic l with addition of magnesium-based alkaline agent
By subjecting η water to biological nitrification and denitrification treatment and then adding Fe" or AI" type flocculants for flocculation treatment, the amount of alkaline agent used in the flocculation process can be significantly reduced. That is, the magnesium-based alkaline agent performs two functions: removing po4''- and acting as a ρ1) regulator for the flocculation process.
■ 膜分離工程が一工程ですみ、従来の膜分離方式に比
べ、膜分離工程のランニングコスト イニシャルコスト
が半減する。■ The membrane separation process is a single step, and the initial cost of running the membrane separation process is halved compared to conventional membrane separation methods.
■ 有機性汚水中のＰＯａ”と有機物が、ＮＩｌ、Ｍｇ
ＰＯ。■ POa” and organic matter in organic wastewater are NIl, Mg
P.O.
を高４度に含んだ低水分の有機性汚泥脱水ケーキとして
回収されるので、リン、有機物を資源として肥料などに
利用でき、従来の膜分離方式では得られない重要効果で
ある。Since it is recovered as a low-moisture organic sludge dehydrated cake that contains phosphorus at a high 4 degrees Celsius, the phosphorus and organic matter can be used as resources for fertilizers, etc., which is an important effect that cannot be obtained with conventional membrane separation methods.
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
。
ｌ・・・し尿、２・・・余剰濃縮スラリ、３・・・マグ
ネシウム系アルカリ剤、４・・・ポリマ、５・・・ウェ
ッジワイヤスクリーン、６・・・スクリーン分離ンク泥
、７・・・機械脱水機、８・・・脱水ケーキ、９・・・
スクリーン分離液、１０・・・生物学的硝化脱窒素処理
工程、１１・・・活性汚泥スラリ、１２・・・Ｆｅ”系
又はへ１３゛系凝集剤、１３・・・膜モジュール、１４
・・・＋１１Ａｉ３過水、１５・・・／店縮スラリ。FIG. 1 is a flow sheet showing one embodiment of the present invention. l... Human waste, 2... Excess concentrated slurry, 3... Magnesium-based alkaline agent, 4... Polymer, 5... Wedge wire screen, 6... Screen separation ink mud, 7... Mechanical dehydrator, 8... Dehydrated cake, 9...
Screen separation liquid, 10... Biological nitrification and denitrification treatment process, 11... Activated sludge slurry, 12... Fe'' type or He13'' type flocculant, 13... Membrane module, 14
...+11Ai3 superhydration, 15.../store shrinkage slurry.
Claims (1)
凝集剤を添加し混和したのち固液分離し、得られた分離
液を生物学的硝化脱窒素処理工程にて処理し、該工程内
もしくは該工程から流出する微生物スラリにＦｅ＾３＾
＋系又はＡｌ＾３＾＋系凝集剤を添加して凝集せしめ、
該凝集スラリを膜分離し、分離された濃縮スラリの一部
を前記生物学的硝化脱窒素処理工程へ返送すると共に、
残部を前記有機性汚水に混合することを特徴とする有機
性汚水の処理方法。(1) After adding and mixing a magnesium-based alkaline agent and a polymer flocculant to organic wastewater, solid-liquid separation is performed, and the resulting separated liquid is treated in a biological nitrification and denitrification treatment process. Fe^3^ is present in the microbial slurry flowing out from the process.
+ type or Al^3^+ type flocculant is added to cause flocculation,
The flocculated slurry is membrane separated, and a part of the separated concentrated slurry is returned to the biological nitrification and denitrification treatment step,
A method for treating organic sewage, comprising mixing the remainder with the organic sewage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63123920A JPH01293196A (en) | 1988-05-23 | 1988-05-23 | Treatment of organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63123920A JPH01293196A (en) | 1988-05-23 | 1988-05-23 | Treatment of organic sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01293196A true JPH01293196A (en) | 1989-11-27 |
| JPH0431760B2 JPH0431760B2 (en) | 1992-05-27 |
Family
ID=14872612
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63123920A Granted JPH01293196A (en) | 1988-05-23 | 1988-05-23 | Treatment of organic sewage |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01293196A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07124571A (en) * | 1993-11-04 | 1995-05-16 | Ngk Insulators Ltd | Treatment process for organic drainage |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56129084A (en) * | 1980-03-13 | 1981-10-08 | Ebara Infilco Co Ltd | Disposal of organic waste water containing phosphoric acid |
| JPS5948157A (en) * | 1982-08-09 | 1984-03-19 | ユニロイヤル・インコ−ポレ−テツド | Coextruded product |
| JPS5949896A (en) * | 1982-09-16 | 1984-03-22 | Ebara Infilco Co Ltd | Treatment of organic waste water |
-
1988
- 1988-05-23 JP JP63123920A patent/JPH01293196A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56129084A (en) * | 1980-03-13 | 1981-10-08 | Ebara Infilco Co Ltd | Disposal of organic waste water containing phosphoric acid |
| JPS5948157A (en) * | 1982-08-09 | 1984-03-19 | ユニロイヤル・インコ−ポレ−テツド | Coextruded product |
| JPS5949896A (en) * | 1982-09-16 | 1984-03-22 | Ebara Infilco Co Ltd | Treatment of organic waste water |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07124571A (en) * | 1993-11-04 | 1995-05-16 | Ngk Insulators Ltd | Treatment process for organic drainage |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0431760B2 (en) | 1992-05-27 |
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