JPS6254080B2 - - Google Patents
Info
- Publication number
- JPS6254080B2 JPS6254080B2 JP55158433A JP15843380A JPS6254080B2 JP S6254080 B2 JPS6254080 B2 JP S6254080B2 JP 55158433 A JP55158433 A JP 55158433A JP 15843380 A JP15843380 A JP 15843380A JP S6254080 B2 JPS6254080 B2 JP S6254080B2
- Authority
- JP
- Japan
- Prior art keywords
- activated carbon
- treatment
- water
- sludge
- concentrated
- 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.)
- Expired
Links
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- 238000000034 method Methods 0.000 claims description 40
- 239000010802 sludge Substances 0.000 claims description 32
- 239000002351 wastewater Substances 0.000 claims description 13
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 239000004576 sand Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 3
- 229920006318 anionic polymer Polymers 0.000 claims description 2
- 229920000642 polymer Polymers 0.000 claims description 2
- 239000003463 adsorbent Substances 0.000 claims 1
- 238000001914 filtration Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000010800 human waste Substances 0.000 description 6
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 5
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 5
- 239000011268 mixed slurry Substances 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000003756 stirring Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- -1 for example Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000003077 lignite Substances 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241000565357 Fraxinus nigra Species 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Water Treatment By Sorption (AREA)
Description
【発明の詳細な説明】
本発明は廃水の高度処理方法、詳しくは、有機
性汚水を生物学的硝化脱窒素法で処理した処理水
を高度処理する方法に関するものである。
従来、廃水の高度処理においては、放流先の環
境問題から、その最終処理水中のBOD、COD、
色度、窒素およびリン等を可能な限り減少させる
ことが求められている。
ところで、BOD成分の含有濃度が高い廃水は
まず生物処理されるが、この廃水に含有される窒
素をも除去しなければならない場合は生物学的硝
化脱窒素法によつて処理するのが通例である。廃
水として例えばし尿を無希釈で生物学的硝化脱窒
素法で処理した場合窒素分についてはほぼ満足で
きるまで除去できるが、他の成分については更に
高度の処理が必要である。
本発明はこのような要求にこたえ汚水中の不純
物成分を効率よく除去する方法を提供することを
目的とするものである。
すなわち本発明は、廃水を生物学的硝化脱窒素
工程にて処理し、該生物学的硝化脱窒素工程の処
理水と余剰汚泥との混合スラリーに、少なくとも
無機凝集剤及び少なくとも粉末活性炭を添加して
濃縮工程にて濃縮スラツジと濃縮分離水に分離
し、前記濃縮スラツジを機械的脱水工程で脱水し
て脱水分離水と脱水ケーキに分離すると共に、前
記濃縮分離水を粒状活性炭処理工程を含む後処理
工程に導くことを特徴とする廃水の高度処理方法
である。
本発明の実施態様を図面に基づいて説明する
と、し尿１は、まず生物学的硝化脱窒素工程２に
よつて処理される。この脱窒素工程２の汚泥濃度
を一定濃度に調整するため、生物処理槽内の汚泥
の一部が遠心分離機３に流入し、分離汚泥４と分
離水５に分離され、分離汚泥４は脱窒素工程２へ
返送される。一方、分離水５は脱窒素工程２から
の流出スラリー６に混合される。この流出スラリ
ー６は従来の活性汚泥法のように最終沈殿池にお
いて活性汚泥を分離した上澄水を意味するのでは
なく、余剰汚泥を含有するスラリーを意味する。
次に、分離水５と流出スラリー６とを混合した
混合スラリー７に粉末活性炭８を添加して所定時
間接触撹拌した後、無機凝集剤を含む凝集剤９を
添加し凝集反応させる。接触槽１０からの流出液
は、必要があれば中和剤により中和された後、濃
縮槽１１にて濃縮スラツジ１３と濃縮分離水１２
に分離される。
濃縮槽１１にて分離された濃縮分離水１２は砂
過塔１９を経た後、粒状活性炭塔２１により処
理され、高度処理水２２として系外へ排出され
る。
一方、濃縮スラツジ１３は機械的脱水工程１４
にて脱水分離水１５と脱水ケーキ１６に分離さ
れ、脱水分離水１５は必要があれば濃縮分離水１
２と混合され、後続の処理が施される。
本発明は、このように汚泥処理工程を水処理工
程中に組み込んで構成したプロセスを採用してお
り、従来の方法が余剰汚泥を水処理工程と別系統
で処理するプロセスに基づいているのと比べ対照
的である。すなわち、本発明では、接触槽１０に
おいて生物処理水についての水の浄化と汚泥脱水
性向上のための処理が同時に達成され従来のよう
に汚泥脱水用の脱水助剤と凝集沈殿用の凝集剤を
各々別個に添加する必要がなくなるという利点が
得られる。つまり、混合スラリー７に対し粉末活
性炭８を添加して所定時間撹拌した後、凝集剤９
を添加して処理すると生物処理水の水の浄化が行
なわれると共に汚泥の脱水性の向上が達成される
のである。
本発明では接触槽１０において粉末活性炭８を
使用する。汚泥の脱水性の向上をはかることのみ
を目的とする場合には、石炭（亜炭、褐炭、瀝青
炭、無煙炭等を含む）、木材、籾殻、石油系残
渣、パルプ工場の黒灰等の炭素質物質を代用して
もよいのであるが、汚泥の脱水性の向上と共に水
の浄化をはかるには廃水中の不純物としての有機
物を吸着除去する作用をもつ粉末活性炭を使用す
る必要がある。従つて上記の炭素質物質のうち吸
着作用をも有する物であればいずれでもこれを粉
末活性炭８と併用することができる。
本発明では前記凝集剤９に含まれる無機凝集剤
としては、鉄系のもの又はアルミニウム系のもの
が使用できる（これらの併用も可能）。また鉄系
凝集剤としては、塩化第二鉄、硫酸第二鉄、硫酸
第一鉄、ポリ硫酸鉄のいずれでも利用できるが塩
化第二鉄が最も効果的である。また、凝集剤９と
して無機凝集剤を単独使用することができるが、
これとノニオン系ポリマー又はアニオン系ポリマ
ーを併用してもよい。
なお、接触槽１０において、粉末活性炭８と凝
集剤９と添加する順序は粉末活性炭―凝集剤、凝
集剤―粉末活性炭、凝集剤―粉末活性炭―凝集剤
のいずれも適用することができ、また、この両者
を同時に添加することも可能であることはいうま
でもない。
前記濃縮槽１１からの濃縮スラツジ１３は機械
的脱水工程１４により脱水されるのであるが、こ
こでの汚泥の脱水性は接触槽１０において加えた
粉末活性炭８の添加量に左右され、その添加量が
多ければ多いほど汚泥の脱水性は向上する。しか
しながら、本発明においては粉末活性炭８によつ
て水の浄化を図ることとしているので、粉末活性
炭８の添加量は後続する高度処理工程を最も効果
的に運転するには中間段階における水質をいくら
にしたいかによつて決定するが、その量は例えば
後記実施例に示す如く、粉末活性炭1000〜2000
mg／塩化第二鉄2000〜4000mg／で、脱水ケー
キの含水率65〜70％（機械的脱水工程１４にフイ
ルタープレスを使用）であり、接触処理後の濃縮
槽１１で分離された濃縮分離水１２の水質は
BOD20〜30mg／、SS20〜30mg／、COD50〜
80mg／、色度50〜100度であつた。
かように、し尿の高度処理においてはCOD成
分をいかに経済的に減少させるかが大きなポイン
トとなる。
前記粒状活性炭処理工程は、砂過処理水２０
中に残留する汚染物を除去するためのものであ
り、ポリツシヤーとしてのこの粒状活性炭処理工
程の吸着方式は通常の固定床式で十分であるが、
更に吸着効率を高めたいとき又は前処理段階での
処理が不十分でSS等が多く残存する危険性があ
るときは、粒状活性炭塔２１の流入水は塔頂より
供給して活性炭充填層を下向流で通水し処理水を
塔底より抜き出し、活性炭の移動は通水方向と逆
にする。いわゆる逆移動床式吸着方式を適用する
と、充填時に塔内を逆洗することになるので更に
効率的な吸着方式となる。
また本発明においては、通常は上記のように濃
縮分離水１２を直接粒状活性炭処理するが、必要
があれば濃縮分離水１２を化学酸化処理工程１７
で処理した後、化学酸化処理水１８を粒状活性炭
処理することも可能である。化学酸化処理工程１
７には酸化剤として過酸化水素、オゾン、塩素等
が使用でき、これらの併用も可能である。
以上述べたように本発明によれば、合理的にか
つ効率よく廃水の高度処理を行なうことができ、
BOD、COD等の低い極めて良質の最終処理水が
得られる利点がある。
次に本発明の実施例について記す。
実施例
前記実施態様の説明で引用したフローシートに
則して後記する表に示す性状のし尿を0.5m3／日
の処理量で無希釈処理した。各工程の処理条件は
次のとおりである。
１ 生物学的硝化脱窒素工程
(1) 滞留時間
第１脱窒素槽 １日
硝化槽 ２日
第２脱窒素槽 １日
(2) その他
水 温 25〜32℃
MLSS 17000〜22000mg／
硝化液循環比 10〜30倍
汚泥返送方法 遠心分離機使用
２ 接触処理工程
粉末活性炭 1000〜2000mg／
塩化第二鉄 2000〜4000mg／
中和剤 消石灰
接触時間 ５〜30分
３ 濃縮工程
重力式シツクナー 固形物負荷
50Kg／m2・日
４ 機械的脱水工程
全自動フイルタープレス
５ 粒状活性炭処理工程
カラム大きさ 5.0cm〓×200cmL
流速（SV） 0.5〜1.5
活性炭量 ２
まず、し尿を生物学的硝化脱窒素工程で処理し
た。次に、該脱窒素工程から発生する余剰汚泥を
混合した混合スラリー液（SS濃度約10000〜
15000mg／）に粉末活性炭1000〜2000mg／と
塩化第二鉄2000〜4000mg／を添加し、PH4.5〜
5.5に維持しながら５〜30分間撹拌した後、重力
式シツクナーで固液分離し、17000〜22000mg／
の濃縮スラツジと濃縮分離水を得た。この濃縮ス
ラツジを全自動フイルタープレスで脱水した結
果、含水率65〜70％の脱水ケーキが得られた。
一方、濃縮分離水は砂過塔を経た後、粒状活
性炭塔の流入水とした。
かくて得られた濃縮分離水と粒状活性炭処理水
（最終処理水）の性状、水質は下表のとおりであ
つた。
【表】DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for advanced treatment of wastewater, and more particularly, to a method for advanced treatment of treated water obtained by treating organic wastewater by a biological nitrification and denitrification method. Conventionally, in advanced wastewater treatment, BOD, COD, and
It is desired to reduce chromaticity, nitrogen, phosphorus, etc. as much as possible. By the way, wastewater with a high concentration of BOD components is first subjected to biological treatment, but if the nitrogen contained in this wastewater must also be removed, it is usually treated using biological nitrification and denitrification methods. be. If wastewater, for example, human waste, is treated without dilution by biological nitrification and denitrification, the nitrogen content can be removed to a nearly satisfactory level, but other components require more advanced treatment. The object of the present invention is to provide a method for efficiently removing impurity components from wastewater in response to such demands. That is, the present invention treats wastewater in a biological nitrification and denitrification process, and adds at least an inorganic flocculant and at least powdered activated carbon to a mixed slurry of treated water and excess sludge in the biological nitrification and denitrification process. The concentrated sludge is separated into concentrated sludge and concentrated separated water in a concentration step, and the concentrated sludge is dehydrated in a mechanical dehydration step to be separated into dehydrated separated water and dehydrated cake, and the concentrated separated water is subjected to a granular activated carbon treatment step. This is an advanced treatment method for wastewater, which is characterized by introducing the wastewater into a treatment process. An embodiment of the present invention will be described based on the drawings. Human waste 1 is first treated in a biological nitrification and denitrification process 2. In order to adjust the sludge concentration in this denitrification process 2 to a constant concentration, a part of the sludge in the biological treatment tank flows into the centrifuge 3 and is separated into separated sludge 4 and separated water 5, and the separated sludge 4 is denitrified. Returned to nitrogen process 2. Meanwhile, the separated water 5 is mixed into the effluent slurry 6 from the denitrification step 2. This effluent slurry 6 does not mean supernatant water from which activated sludge has been separated in a final settling tank as in the conventional activated sludge method, but means a slurry containing excess sludge. Next, powdered activated carbon 8 is added to mixed slurry 7, which is a mixture of separated water 5 and effluent slurry 6, and after contact stirring for a predetermined time, a flocculant 9 containing an inorganic flocculant is added to cause a flocculation reaction. The effluent from the contact tank 10 is neutralized with a neutralizing agent if necessary, and then transferred to a concentration tank 11 where it is converted into concentrated sludge 13 and concentrated separated water 12.
separated into Concentrated and separated water 12 separated in the concentration tank 11 passes through a sand filter tower 19, is treated in a granular activated carbon tower 21, and is discharged to the outside of the system as highly treated water 22. On the other hand, the concentrated sludge 13 is processed through mechanical dewatering process 14.
The dehydrated separated water 15 is separated into dehydrated separated water 15 and dehydrated cake 16, and the dehydrated separated water 15 is converted into concentrated separated water 1 if necessary.
2 and subjected to subsequent processing. The present invention employs a process in which the sludge treatment process is incorporated into the water treatment process, and is different from the conventional method, which is based on a process in which excess sludge is treated in a separate system from the water treatment process. Compare and contrast. That is, in the present invention, water purification of biologically treated water and treatment for improving sludge dewatering properties are simultaneously achieved in the contact tank 10, and a dewatering aid for sludge dewatering and a flocculant for flocculating sedimentation are used as in the conventional method. The advantage is that there is no need to add each separately. That is, after adding powdered activated carbon 8 to mixed slurry 7 and stirring for a predetermined time, flocculant 9
When treated with the addition of sludge, the biologically treated water is purified and the dewaterability of the sludge is improved. In the present invention, powdered activated carbon 8 is used in the contact tank 10. If the sole purpose is to improve the dewaterability of sludge, carbonaceous materials such as coal (including lignite, lignite, bituminous coal, anthracite, etc.), wood, rice husk, petroleum residue, black ash from pulp mills, etc. However, in order to improve the dehydration properties of sludge and purify water, it is necessary to use powdered activated carbon, which has the ability to adsorb and remove organic matter as impurities in wastewater. Therefore, any carbonaceous material mentioned above that also has an adsorption effect can be used in combination with the powdered activated carbon 8. In the present invention, as the inorganic flocculant contained in the flocculant 9, an iron-based one or an aluminum-based one can be used (a combination of these can also be used). Further, as the iron-based flocculant, any of ferric chloride, ferric sulfate, ferrous sulfate, and polyferrous sulfate can be used, but ferric chloride is the most effective. Moreover, an inorganic flocculant can be used alone as the flocculant 9, but
This may be used in combination with a nonionic polymer or an anionic polymer. In addition, in the contact tank 10, the order in which the powdered activated carbon 8 and the flocculant 9 are added can be either powdered activated carbon-flocculant, flocculant-powdered activated carbon, or flocculant-powdered activated carbon-flocculant; It goes without saying that it is also possible to add both at the same time. The concentrated sludge 13 from the thickening tank 11 is dewatered in a mechanical dewatering step 14, and the dewatering performance of the sludge here depends on the amount of powdered activated carbon 8 added in the contact tank 10, and the amount The greater the amount, the better the dewaterability of sludge will be. However, in the present invention, water is purified using powdered activated carbon 8, so the amount of powdered activated carbon 8 added should be adjusted to the desired water quality in the intermediate stage in order to operate the subsequent advanced treatment process most effectively. The amount is determined depending on what is desired, but the amount is, for example, 1000 to 2000 powdered activated carbon, as shown in the examples below.
mg/ferric chloride 2000 to 4000 mg/, the moisture content of the dehydrated cake is 65 to 70% (a filter press is used in the mechanical dehydration step 14), and the concentrated separated water is separated in the concentration tank 11 after the contact treatment. 12 water quality is
BOD20~30mg/, SS20~30mg/, COD50~
80mg/, chromaticity was 50-100 degrees. Thus, the key point in advanced treatment of human waste is how to economically reduce COD components. In the granular activated carbon treatment step, sand filter treated water 20
The purpose is to remove contaminants that remain in the granular activated carbon, and the adsorption method for this granular activated carbon treatment process as a polisher is a normal fixed bed type.
When it is desired to further increase the adsorption efficiency, or when there is a risk that a large amount of SS etc. remains due to insufficient treatment in the pre-treatment stage, the inflow water of the granular activated carbon tower 21 is supplied from the top of the tower to flow down the activated carbon packed bed. Water is passed in a countercurrent flow, and treated water is extracted from the bottom of the tower, with activated carbon moving in the opposite direction to the water flow. When a so-called reverse moving bed adsorption system is applied, the interior of the column is backwashed during filling, resulting in a more efficient adsorption system. Further, in the present invention, normally the concentrated separated water 12 is directly treated with granular activated carbon as described above, but if necessary, the concentrated separated water 12 is treated in the chemical oxidation treatment step 17.
It is also possible to treat the chemically oxidized water 18 with granular activated carbon after the treatment. Chemical oxidation treatment step 1
For No. 7, hydrogen peroxide, ozone, chlorine, etc. can be used as an oxidizing agent, and a combination of these can also be used. As described above, according to the present invention, advanced treatment of wastewater can be carried out rationally and efficiently.
It has the advantage of producing extremely high quality final treated water with low BOD, COD, etc. Next, examples of the present invention will be described. Example In accordance with the flow sheet cited in the description of the embodiment, human waste having the properties shown in the table below was treated without dilution at a treatment rate of 0.5 m 3 /day. The processing conditions for each step are as follows. 1 Biological nitrification and denitrification process (1) Residence time 1st denitrification tank 1 day Nitrification tank 2 days 2nd denitrification tank 1 day (2) Other water temperature 25-32℃ MLSS 17000-22000mg/Nitrified liquid circulation ratio 10-30 times sludge return method: Use of centrifuge 2 Contact treatment process Powdered activated carbon 1000-2000mg/ Ferric chloride 2000-4000mg/ Neutralizing agent Slaked lime contact time 5-30 minutes 3 Concentration process Gravity type thickener Solid loading
50Kg/m 2・day 4 Mechanical dehydration process Fully automatic filter press 5 Granular activated carbon treatment process Column size 5.0cm〓×200cm L flow rate (SV) 0.5 to 1.5 Activated carbon amount 2 First, human waste is subjected to biological nitrification and denitrification process Processed with. Next, a mixed slurry liquid containing surplus sludge generated from the denitrification process (SS concentration of about 10,000 ~
Add powdered activated carbon 1000-2000mg/ and ferric chloride 2000-4000mg/ to 15000mg/) to make the pH 4.5~
After stirring for 5 to 30 minutes while maintaining the temperature of
A concentrated sludge and concentrated separated water were obtained. This concentrated sludge was dehydrated using a fully automatic filter press, resulting in a dehydrated cake with a water content of 65-70%. On the other hand, the concentrated separated water passed through a sand filter tower and was then used as the inflow water of the granular activated carbon tower. The properties and quality of the concentrated separated water and granular activated carbon treated water (final treated water) thus obtained were as shown in the table below. 【table】
図面は本発明の実施態様を示す系統説明図であ
る。
１…し尿、２…脱窒素工程、３…遠心分離機、
４…分離汚泥、５…分離水、６…流出スラリー、
７…混合スラリー、８…粉末活性炭、９…凝集
剤、１０…接触槽、１１…濃縮槽、１２…濃縮分
離水、１３…濃縮スラツジ、１４…機械的脱水工
程、１５…脱水分離水、１６…脱水ケーキ、１７
…化学酸化処理工程、１８…化学酸化処理水、１
９…砂過塔、２０…砂過処理水、２１…粒状
活性炭塔、２２…高度処理水。
The drawings are system explanatory diagrams showing embodiments of the present invention. 1... Human waste, 2... Denitrification process, 3... Centrifugal separator,
4... Separated sludge, 5... Separated water, 6... Outflow slurry,
7...Mixed slurry, 8...Powdered activated carbon, 9...Flocculant, 10...Contact tank, 11...Concentration tank, 12...Concentrated separated water, 13...Concentrated sludge, 14...Mechanical dehydration process, 15...Dehydrated separated water, 16 ...Dehydrated cake, 17
...Chemical oxidation treatment step, 18...Chemical oxidation treatment water, 1
9... Sand filter tower, 20... Sand filter treated water, 21... Granular activated carbon tower, 22... Highly treated water.
Claims (1)
したのち、該生物学的硝化脱窒素工程の処理水と
余剰汚泥との混合スラリーに無機凝集剤を含む凝
集剤及び粉末活性炭を含む吸着剤を添加して処理
し、該処理液を濃縮工程にて濃縮スラツジと濃縮
分離水に分離し、前記濃縮スラツジを機械的脱水
工程で脱水すると共に、前記濃縮分離水を粒状活
性炭処理工程を含む後処理工程に導くことを特徴
とする有機性廃水の高度処理方法。 ２ 前記凝集剤として無機凝集剤とノニオン系ポ
リマー又はアニオン系ポリマーを併用する特許請
求の範囲第１項記載の方法。 ３ 前記後処理工程が、前段工程としての化学酸
化処理工程と後段工程としての粒状活性炭処理工
程からなるものである特許請求の範囲第１項又は
第２項記載の方法。 ４ 前記後処理工程が、前段工程としての化学酸
化処理工程、中段工程としての砂過工程及び後
段工程としての粒状活性炭処理工程からなるもの
である特許請求の範囲第１項又は第２項記載の方
法。[Claims] 1. After treating organic wastewater in a biological nitrification and denitrification process, a flocculant containing an inorganic flocculant and An adsorbent containing powdered activated carbon is added to the treatment, the treated liquid is separated into concentrated sludge and concentrated separated water in a concentration step, the concentrated sludge is dehydrated in a mechanical dehydration step, and the concentrated separated water is granulated. An advanced treatment method for organic wastewater, characterized in that it is led to a post-treatment process including an activated carbon treatment process. 2. The method according to claim 1, wherein an inorganic flocculant and a nonionic polymer or an anionic polymer are used together as the flocculant. 3. The method according to claim 1 or 2, wherein the post-treatment step comprises a chemical oxidation treatment step as a first step and a granular activated carbon treatment step as a second step. 4. The method according to claim 1 or 2, wherein the post-treatment step consists of a chemical oxidation treatment step as a first step, a sand filtering step as a middle step, and a granular activated carbon treatment step as a second step. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55158433A JPS5781891A (en) | 1980-11-11 | 1980-11-11 | High-degree treatment of organic waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55158433A JPS5781891A (en) | 1980-11-11 | 1980-11-11 | High-degree treatment of organic waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5781891A JPS5781891A (en) | 1982-05-22 |
| JPS6254080B2 true JPS6254080B2 (en) | 1987-11-13 |
Family
ID=15671649
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP55158433A Granted JPS5781891A (en) | 1980-11-11 | 1980-11-11 | High-degree treatment of organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5781891A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6320092A (en) * | 1986-07-14 | 1988-01-27 | Sanee Kogyo Kk | Solid-liquid separator |
| JP6823513B2 (en) * | 2017-03-21 | 2021-02-03 | オルガノ株式会社 | Operation method of sludge blanket type coagulation sedimentation device and sludge blanket type coagulation sedimentation device |
-
1980
- 1980-11-11 JP JP55158433A patent/JPS5781891A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5781891A (en) | 1982-05-22 |
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