JPH0317560B2 - - Google Patents
Info
- Publication number
- JPH0317560B2 JPH0317560B2 JP63299496A JP29949688A JPH0317560B2 JP H0317560 B2 JPH0317560 B2 JP H0317560B2 JP 63299496 A JP63299496 A JP 63299496A JP 29949688 A JP29949688 A JP 29949688A JP H0317560 B2 JPH0317560 B2 JP H0317560B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- activated sludge
- treatment
- nitrification
- denitrification
- 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 - Lifetime
Links
- 239000010802 sludge Substances 0.000 claims description 86
- 238000011282 treatment Methods 0.000 claims description 31
- 238000000034 method Methods 0.000 claims description 25
- 239000012535 impurity Substances 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000010800 human waste Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 239000000356 contaminant Substances 0.000 claims description 7
- 229920000642 polymer Polymers 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 238000005189 flocculation Methods 0.000 claims description 6
- 230000016615 flocculation Effects 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 238000005273 aeration Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 235000019645 odor Nutrition 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 4
- 238000013019 agitation Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000001580 bacterial effect Effects 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 230000001546 nitrifying effect Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000002776 aggregation Effects 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 229920006317 cationic polymer Polymers 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 230000008719 thickening Effects 0.000 description 2
- 239000003570 air Substances 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229920006318 anionic polymer Polymers 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 159000000014 iron salts Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- 239000005518 polymer electrolyte Substances 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Description
〔産業上の利用分野〕
本発明は、し尿系汚水の硝化脱窒素活性汚泥処
理において発生する余剰汚泥あるいは該余剰汚泥
と凝集汚泥との混合汚泥の脱水方法に関するもの
である。
〔従来の技術〕
一般にし尿系汚水（以下し尿とする）の活性汚
泥処理法（酸化処理）では、活性汚泥処理（二次
処理）を円滑に行うために、前処理（一次処理）
として夾雑物除去工程でし尿中の夾雑物をスクリ
ーン等で別し、その後の液（液）を活性汚泥
処理する。この活性汚泥処理法で排泥される汚泥
は、前処理で別された夾雑物、活性汚泥装置の
余剰汚泥、さらに凝集処理も行う場合には凝集汚
泥の三つに大別される。除去された夾雑物はスク
リユープレス、フイルタプレスなどで含水率60％
程度にまで脱水されたのち通常直接焼却され、余
剰汚泥は単独あるいは凝集汚泥と混合されたの
ち、高分子凝集剤によつて凝集され、脱水、乾
燥、焼却されている。
〔発明が解決しようとする課題〕
ところで、活性汚泥処理の余剰汚泥は、菌体を
主成分とする微細な有機固形分から構成されてお
り、菌体内の細胞液、菌体外の粘物質などの遊離
し難い水を保有しているため、上記除去された夾
雑物に比べ脱水性は極めて悪い。また、現在広く
普及しているAl3+、Fe3+による凝集処理の汚泥
も難脱水性で凝集処理の欠点の一つとなつてい
る。例えば、し尿処理装置からの余剰汚泥と凝集
汚泥との混合汚泥の脱水ケーキ含水率は、デカン
タ式遠心分離機で85％、ベルトプレスで80〜82％
程度にしかならない。脱水ケーキの含水率が高く
なると、単に水分蒸発のエネルギを多量に必要と
するばかりでなく、粘稠性が増加してケーキの裁
断が不充分となるため、乾燥用気体と脱水ケーキ
の接触面積が減少し、乾燥効率が低下し、さらに
は乾燥炉の壁に付着し連続乾燥が不可能となる。
以上のような欠点を解決するため、脱水ケーキ含
水率を確実に80％以下にする経済的な方法が種々
研究されているが、いまだ未解決のままである。
しかも活性汚泥処理における前処理たる夾雑物
除去工程は前述のごとく、二次処理の円滑化のた
めに必要なものであるが、し尿のBOD、CODの
他に窒素分も除去する硝化脱窒素活性汚泥法にと
つてはとりわけ重要である。活性汚泥が硝化能を
有するためには硝化菌が曝気槽（硝化工程）から
洗出しない汚泥齢（日）（曝気槽汚泥量／余剰汚
泥量）を保たなければならないが、硝化菌の増殖
速度は0.173／日（15℃）で通常のBOD酸化菌に
比べてはるかに小さく、次式
As＝Ys／ΔYs≦１／μ
As：汚泥齢（日）
Ys：曝気槽汚泥量（Kg）
ΔYs：余剰汚泥量（Kg／日）
μ：硝化菌の増殖速度（／日）
に示される硝化のための汚泥齢を満足するために
は、曝気槽に流入する生物不活性の夾雑物（浮遊
固形物）を除去し、余剰汚泥量（引抜汚泥量）を
減らすように努めなければならない。そのため、
前処理の過装置の目開きは次第に狭くされてき
ている。しかし、比較的粗いSSであるし尿の夾
雑物を、活性汚泥処理の前段で除去すればするほ
ど発生する余剰汚泥を構成する固形分は微細化さ
れ、難脱水性の汚泥へと転じ、硝化脱窒素活性汚
泥処理の大きな問題となつている。さらにまた、
脱水ケーキの悪臭が強く、事後処理に支障を来し
ている。
以上のように、し尿の活性汚泥処理とりわけ硝
化脱窒素活性汚泥処理にとつて、余剰汚泥、凝集
汚泥の難脱水性は宿命的な欠点として問題となつ
ている。
本発明は、これら従来の問題点を解消し含水率
の低いかつ悪臭の少ない脱水ケーキを容易に得ら
れ、且つ著しく経済的なコストで処理される有効
な汚泥脱水方法を提供することを目的としたもの
である。
〔課題を解決するための手段〕
本発明は、し尿系汚水をスクリーンなどの機械
式固液分離法を用いた夾雑物除去工程にて夾雑物
を除去し、得られた汚水を固液分離することなく
硝化脱窒素活性汚泥処理工程に導き、活性汚泥と
混合曝気したのち、活性汚泥と処理水とに分離し
て該活性汚泥を返送して硝化脱窒素活性汚泥処理
すると共に、該硝化脱窒素活性汚泥処理工程から
排出される余剰活性汚泥あるいは該余剰活性汚泥
と前記処理水の凝集汚泥との混合汚泥に、空気、
酸素又はオゾン化空気の少なくともいずれかのガ
ス撹拌によつて前記夾雑物除去工程で除去された
夾雑物を混入混合し、さらに高分子凝集剤を添加
して凝集させ、プレス型脱水機で脱水することを
特徴とする汚泥の脱水方法である。
〔作用〕
本発明の作用を一実施態様を示す第１図を参照
しつつ説明すると、前処理である夾雑物除去工程
２に流入したし尿１は別（スクリーニング）さ
れ、液３となつて固液分離されることなく、
液３中に生分解性のよいコロイダルな粒子を含ん
だまま硝化脱窒素活性汚泥処理工程４に流入し、
前記コロイダル粒子等を水素供与体として有効利
用して脱窒素効果が促進され、浄化されたのち、
凝集処理工程６に流入し、凝集処理される。この
硝化脱窒素活性汚泥処理工程４の余剰汚泥８と凝
集処理工程６の凝集汚泥９は濃縮槽１１で濃縮さ
れたのち、夾雑物除去工程２から移送される夾雑
物１０と汚泥貯留槽１２において、残留する
BOD分の除去、夾雑物の同伴された脱水性を妨
害するコロイダルなSSの酸化分解および脱臭を
兼ねて空気、酸素あるいはオゾン化空気の少なく
ともいずれかのガス撹拌によつて混合されたの
ち、凝集槽１３で高分子凝集剤１４の添加によつ
て凝集され、プレス型の脱水機１５で脱水処理さ
れ含水率の低いかつ悪臭の少ない脱水ケーキ１６
を効率よく得られるものである。
前記夾雑物除去工程２で発生する夾雑物１０は
汚泥に対し10〜40重量％、好ましくは20〜30重量
％を直接汚泥貯留槽１２に移送して混合するが、
夾雑物１０を水洗したほうが悪臭の発生をさらに
防止し、また夾雑物に同伴された脱水性を妨害す
るコロイダルなSSを洗い出すうえで好ましい。
なお、前記汚泥貯留槽１２の混合はガス撹拌と機
械撹拌等の併用でもよい。
なお前記高分子凝集剤１４としては、汚泥によ
つてポリアクリルアミドのカチオン変形物などの
カチオン性高分子凝集剤、アニオン性高分子凝集
剤又はノニオン性高分子凝集剤が単独又組み合わ
せて汚泥乾燥固形物当たり0.1〜2.0％用いられ、
必要に応じ凝集助剤例えば消石灰、高分子電解質
などを併用することもでき、また鉄塩、アルミニ
ウム塩などの無機凝集剤を併用することもでき
る。
また脱水工程で用いられる脱水機１５として
は、ロール又はベルトプレス型脱水機、その他の
プレス型脱水機が選んで用いられる。
これは余剰活性汚泥と夾雑物の混合分布状態が
粗くて、均一でない汚泥を脱水するには脱水機と
してプレス型のものを利用した方が脱水効果が向
上するからである。
〔実施例〕
次に本発明方法と従来法とを比較した実施例を
述べる。
撹拌条件（撹拌時間16時間）：
Ａ：パドル付き機械式回転撹拌機（60r.p.m）
Ｂ：空気、1.5Nm3／m3汚泥・時間
Ｃ：酸素富化空気（酸素含有量50％）、1.0Nm3／
m3汚泥・時間
Ｄ：オゾン化空気（O3濃度20mg／）、1.0Nm3／
m3汚泥・時間
脱水条件：
脱水機：ベルトプレス型脱水機（実験装置布幅
200mm）
布張力 ５Kgｆ／cm
布速度 １ｍ／min
薬注量：カチオン性高分子凝集剤0.8％対SS
これらの結果を表−１に示す。
[Industrial Application Field] The present invention relates to a method for dewatering surplus sludge generated in the nitrification-denitrification activated sludge treatment of night soil wastewater or a mixed sludge of the surplus sludge and flocculated sludge. [Prior art] Generally, in the activated sludge treatment method (oxidation treatment) for night soil wastewater (hereinafter referred to as human waste), pretreatment (primary treatment) is required to smoothly perform activated sludge treatment (secondary treatment).
In the impurity removal process, impurities in the human waste are separated using a screen, etc., and the resulting liquid is treated with activated sludge. The sludge discharged in this activated sludge treatment method is roughly divided into three types: impurities separated by pretreatment, excess sludge from the activated sludge equipment, and flocculated sludge when flocculation treatment is also performed. Removed impurities have a moisture content of 60% using screw press, filter press, etc.
After the sludge has been dehydrated to a certain extent, it is usually directly incinerated, and the surplus sludge is used alone or mixed with flocculated sludge, and then flocculated with a polymer flocculant, dehydrated, dried, and incinerated. [Problems to be Solved by the Invention] By the way, surplus sludge from activated sludge treatment is composed of fine organic solids mainly composed of bacterial cells, and contains cell fluid inside the bacterial cells, slime material outside the bacterial cells, etc. Since it contains water that is difficult to release, its dehydration properties are extremely poor compared to the above-mentioned removed impurities. Furthermore, the sludge produced by flocculation treatment using Al 3+ and Fe 3+ , which is currently widely used, is also difficult to dewater, which is one of the drawbacks of flocculation treatment. For example, the water content of the dehydrated cake of the mixed sludge of excess sludge and flocculated sludge from the human waste treatment equipment is 85% with a decanter centrifuge and 80-82% with a belt press.
It will only be to a certain extent. When the moisture content of the dehydrated cake increases, not only does it require a large amount of energy to evaporate water, but the cake also becomes more viscous and cannot be cut properly. This decreases the drying efficiency, and furthermore, it adheres to the walls of the drying oven, making continuous drying impossible.
In order to solve the above-mentioned drawbacks, various economical methods have been studied to ensure that the moisture content of the dehydrated cake is 80% or less, but the solution remains unsolved. Moreover, as mentioned above, the impurity removal process that is a pretreatment in activated sludge treatment is necessary to facilitate the secondary treatment, but the nitrification and denitrification activity that removes nitrogen as well as BOD and COD from human waste is necessary. This is particularly important for sludge processes. In order for activated sludge to have nitrification ability, it is necessary to maintain a sludge age (days) (aeration tank sludge volume/surplus sludge volume) at which nitrifying bacteria do not wash out from the aeration tank (nitrification process), but the growth of nitrifying bacteria The rate is 0.173/day (15℃), which is much smaller than normal BOD oxidizing bacteria, and is expressed by the following formula: A s = Y s /ΔY s ≦1/μ A s : Sludge age (days) Y s : Aeration tank sludge amount (Kg) ΔY s : Surplus sludge amount (Kg/day) μ: Growth rate of nitrifying bacteria (/day) In order to satisfy the sludge age for nitrification shown in Efforts must be made to remove foreign matter (suspended solids) and reduce the amount of excess sludge (the amount of sludge extracted). Therefore,
The aperture of pretreatment equipment is becoming increasingly narrower. However, the more the relatively coarse SS impurities in human waste are removed in the earlier stages of activated sludge treatment, the more the solid content that makes up the surplus sludge that is generated becomes finer, turning into sludge that is difficult to dewater, and nitrification and dewatering. This has become a major problem in nitrogen activated sludge treatment. Furthermore,
The dehydrated cake has a strong odor, which is interfering with post-processing. As mentioned above, in activated sludge treatment of human waste, particularly in nitrification and denitrification activated sludge treatment, the difficulty in dewatering of excess sludge and flocculated sludge has become a fatal drawback. The purpose of the present invention is to provide an effective sludge dewatering method that solves these conventional problems, easily obtains a dehydrated cake with a low water content and little odor, and can be processed at a significantly economical cost. This is what I did. [Means for Solving the Problems] The present invention removes impurities from human waste wastewater in a contaminant removal process using a mechanical solid-liquid separation method such as a screen, and separates the obtained wastewater into solid-liquid. After being mixed with activated sludge and aerated, the activated sludge is separated into activated sludge and treated water, and the activated sludge is returned for nitrification and denitrification activated sludge treatment. Air,
The impurities removed in the impurity removal step are mixed by gas agitation of at least one of oxygen or ozonized air, and a polymer flocculant is further added to coagulate the mixture, followed by dehydration using a press type dehydrator. This method of dewatering sludge is characterized by the following. [Function] The function of the present invention will be explained with reference to FIG. 1 showing one embodiment. The human waste 1 that has flowed into the impurity removal step 2, which is a pretreatment, is separated (screened), becomes a liquid 3, and is solidified. without liquid separation,
The liquid 3 flows into the nitrification and denitrification activated sludge treatment process 4 while containing colloidal particles with good biodegradability,
After the denitrification effect is promoted and purified by effectively utilizing the colloidal particles etc. as a hydrogen donor,
It flows into an aggregation treatment step 6 and is subjected to an aggregation treatment. The surplus sludge 8 from the nitrification and denitrification activated sludge treatment process 4 and the flocculated sludge 9 from the flocculation treatment process 6 are concentrated in a thickening tank 11, and then transferred to the contaminants 10 and sludge storage tank 12, which are transferred from the contaminant removal process 2. , remain
In order to remove BOD content, oxidize decomposition and deodorize colloidal SS that interferes with dehydration accompanied by impurities, air, oxygen, or ozonized air are mixed by gas agitation, and then coagulated. A dehydrated cake 16 that is flocculated in a tank 13 by adding a polymer flocculant 14 and dehydrated in a press-type dehydrator 15 and has a low moisture content and a low odor.
can be obtained efficiently. The impurities 10 generated in the impurity removal step 2 are directly transferred to the sludge storage tank 12 and mixed in an amount of 10 to 40% by weight, preferably 20 to 30% by weight, based on the sludge.
It is preferable to wash the contaminants 10 with water to further prevent the generation of bad odors and to wash out colloidal SS that is accompanied by the contaminants and interferes with dehydration.
In addition, the mixing in the sludge storage tank 12 may be performed using a combination of gas agitation and mechanical agitation. The polymer flocculant 14 may be a cationic polymer flocculant such as a cationic variant of polyacrylamide, an anionic polymer flocculant, or a nonionic polymer flocculant, either alone or in combination, depending on the sludge. Used at 0.1-2.0% per substance,
If necessary, flocculating aids such as slaked lime and polymer electrolytes can be used in combination, and inorganic flocculants such as iron salts and aluminum salts can also be used in combination. Further, as the dehydrator 15 used in the dehydration process, a roll or belt press type dehydrator or another press type dehydrator is selected and used. This is because in order to dewater sludge where the mixed distribution of excess activated sludge and impurities is rough and not uniform, the dewatering effect will be improved if a press type dehydrator is used as the dehydrator. [Example] Next, an example comparing the method of the present invention and the conventional method will be described. Stirring conditions (stirring time 16 hours): A: Mechanical rotary stirrer with paddle (60r.pm) B: Air, 1.5Nm3 / m3 sludge/time C: Oxygen-enriched air (oxygen content 50%), 1.0Nm 3 /
m3 sludge/time D: Ozonized air ( O3 concentration 20mg/), 1.0Nm3 /
m 3 sludge/time dewatering conditions: Dewatering machine: Belt press type dehydrating machine (experimental equipment cloth width
200mm) Cloth tension: 5Kgf/cm Cloth speed: 1m/min Chemical injection amount: cationic polymer flocculant 0.8% vs. SS These results are shown in Table 1.
以上述べたように、本発明により、含水率の低
い脱水ケーキを得ることができ難脱水性のし尿系
汚水の余剰汚泥、凝集汚泥の脱水性をも改良する
ことができ、また夾雑物の脱水機も不要とするこ
とができると共に、公害防止対策上、有用な処理
が可能となり、その処理コストも経済的で安定し
た作業ができ従来の諸問題を容易に解消すること
ができる利益がある。即ち、夾雑物がスクリーン
などの機械式固液分離装置によつて充分に水が切
られているため、高濃度になつていると共に非繊
維性の粘稠、膠質の浮遊物はスクリーンを通過
し、なおかつ活性汚泥処理で充分に分解あるいは
改質して凝集性が高められたのち、余剰汚泥とし
て引き抜かれるので、含水率の低い脱水ケーキを
得ることができ、乾燥効率が向上し、また水分蒸
発量も少なくなるので脱水ケーキ乾燥用の重油消
費が少なくなり、経済的である。
また、し尿系汚水中のBOD成分が硝化脱窒素
活性汚泥処理工程の前で低減されないので充分な
脱窒が期待できるし、し尿系汚水は夾雑物にのみ
含有されているだけであり、しかも機械式固液分
離により充分水切りされているので、被脱水汚泥
中のし尿系汚水の量はわずかであり、したがつて
悪臭も弱い。
さらに、空気、酸素又はオゾン化空気の少なく
ともいずれかのガス撹拌によつて夾雑物を余剰汚
泥あるいは混合汚泥に混入混合するので残留
BOD成分を除去し、また脱水性を妨害するコロ
イダルなSSを酸化分解し、かつ悪臭も少なくす
ることもできる。
As described above, according to the present invention, it is possible to obtain a dehydrated cake with a low moisture content, and it is also possible to improve the dewaterability of surplus sludge and flocculated sludge, which are difficult to dewater. This method eliminates the need for a machine, enables useful treatment in terms of pollution prevention measures, and has the advantage that the treatment cost is economical, stable work can be done, and various conventional problems can be easily solved. In other words, since the impurities have been sufficiently drained by a mechanical solid-liquid separator such as a screen, they are highly concentrated and non-fibrous, viscous, colloid suspended substances do not pass through the screen. Moreover, after the activated sludge treatment has sufficiently decomposed or modified the flocculation property, it is extracted as surplus sludge, making it possible to obtain a dehydrated cake with a low water content, improving drying efficiency, and reducing water evaporation. Since the amount is also reduced, heavy oil consumption for drying the dehydrated cake is reduced, making it economical. In addition, sufficient denitrification can be expected because the BOD components in human waste water are not reduced before the nitrification and denitrification activated sludge treatment process. Since the water is sufficiently removed by solid-liquid separation, the amount of human waste water in the dewatered sludge is small, and therefore the odor is weak. Furthermore, impurities are mixed into the excess sludge or mixed sludge by stirring at least one of air, oxygen, or ozonized air, so that no residual substances remain.
It can also remove BOD components, oxidize and decompose colloidal SS that interferes with dehydration, and reduce bad odors.
第１図は本発明方法の一実施態様を示す系統説
明図である。
１……し尿、２……夾雑物除去工程、３……
液、４……硝化脱窒素活性汚泥処理工程、５……
硝化脱窒素活性汚泥処理水、６……凝集処理工
程、７……凝集処理水、８……余剰汚泥、９……
凝集汚泥、１０……夾雑物、１１……濃縮槽、１
２……汚泥貯留槽、１３……凝集槽、１４……高
分子凝集剤、１５……脱水機、１６……脱水ケー
キ。
FIG. 1 is a system explanatory diagram showing one embodiment of the method of the present invention. 1... human waste, 2... impurity removal process, 3...
Liquid, 4... Nitrification and denitrification activated sludge treatment process, 5...
Nitrification and denitrification activated sludge treated water, 6... Coagulation treatment step, 7... Coagulation treated water, 8... Excess sludge, 9...
Coagulated sludge, 10... Contaminants, 11... Thickening tank, 1
2... Sludge storage tank, 13... Coagulation tank, 14... Polymer flocculant, 15... Dehydrator, 16... Dehydrated cake.
Claims (1)
離法を用いた夾雑物除去工程にて夾雑物を除去
し、得られた汚水を固液分離することなく硝化脱
窒素活性汚泥処理工程に導き、活性汚泥と混合曝
気したのち、活性汚泥と処理水とに分離して該活
性汚泥を返送して硝化脱窒素活性汚泥処理すると
共に、該硝化脱窒素活性汚泥処理工程から排出さ
れる余剰活性汚泥あるいは該余剰活性汚泥と前記
処理水の凝集汚泥との混合汚泥に、空気、酸素又
はオゾン化空気の少なくともいずれかのガス撹拌
によつて前記夾雑物除去工程で除去された夾雑物
を混入混合し、さらに高分子凝集剤を添加して凝
集させ、プレス型脱水機で脱水することを特徴と
する汚泥の脱水方法。1. Remove impurities from human waste wastewater in a contaminant removal process using a mechanical solid-liquid separation method such as a screen, and guide the obtained wastewater to a nitrification-denitrification activated sludge treatment process without solid-liquid separation. After mixing with activated sludge and aeration, the activated sludge is separated into activated sludge and treated water, and the activated sludge is returned for nitrification and denitrification activated sludge treatment. Mixing the impurities removed in the impurity removal step by stirring at least one of air, oxygen, or ozonized air into the mixed sludge of the excess activated sludge and the flocculated sludge of the treated water, A sludge dewatering method characterized by further adding a polymer flocculant to cause flocculation and dewatering using a press type dehydrator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63299496A JPH01274900A (en) | 1988-11-29 | 1988-11-29 | Method for dehydrating sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63299496A JPH01274900A (en) | 1988-11-29 | 1988-11-29 | Method for dehydrating sludge |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9412879A Division JPS5617690A (en) | 1979-07-24 | 1979-07-24 | Dehydrating method for sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01274900A JPH01274900A (en) | 1989-11-02 |
| JPH0317560B2 true JPH0317560B2 (en) | 1991-03-08 |
Family
ID=17873327
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63299496A Granted JPH01274900A (en) | 1988-11-29 | 1988-11-29 | Method for dehydrating sludge |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01274900A (en) |
-
1988
- 1988-11-29 JP JP63299496A patent/JPH01274900A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01274900A (en) | 1989-11-02 |
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