JPH0647119B2 - Combined treatment method of human waste and septic tank sludge - Google Patents
Combined treatment method of human waste and septic tank sludgeInfo
- Publication number
- JPH0647119B2 JPH0647119B2 JP25005490A JP25005490A JPH0647119B2 JP H0647119 B2 JPH0647119 B2 JP H0647119B2 JP 25005490 A JP25005490 A JP 25005490A JP 25005490 A JP25005490 A JP 25005490A JP H0647119 B2 JPH0647119 B2 JP H0647119B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- septic tank
- membrane
- separation
- human waste
- 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
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、し尿と浄化槽汚泥とを併合処理する方法に関
するものである。TECHNICAL FIELD The present invention relates to a method for treating human waste and septic tank sludge in combination.
〔従来の技術〕 従来のし尿と浄化槽汚泥の併合処理方法のなかで、最も
新しい進歩したプロセスとして評価されているものは、
高負荷脱窒素膜分離方式と呼ばれているプロセスであ
る。これは、し尿と浄化槽汚泥との混合液を無希釈、高
容積負荷で硝化脱窒素処理したのち、限外濾過（ＵＦ）
膜によりＳＳを完全に膜分離し、ＳＳゼロの生物処理水
を得るプロセスである。[Prior Art] Among the conventional combined treatment methods of human waste and septic tank sludge, the one evaluated as the newest advanced process is:
This is a process called the high load denitrification membrane separation method. This is an ultrafiltration (UF) process after nitrifying and denitrifying a liquid mixture of human waste and septic tank sludge with a high volume load.
This is a process to obtain SS-zero biologically treated water by completely separating SS with a membrane.
しかし、前記従来の最新プロセスは、汚水を浄化するプ
ロセスとしては合理的ではあるものの、汚泥処理工程が
旧態依然であり、次のような大きな欠点をもっている。However, although the conventional latest process is rational as a process for purifying sewage, the sludge treatment process is still old and has the following major drawbacks.
即ち、汚泥発生量が１０〜１５kgＳＳ／ｋと極めて多
量であり、しかも難脱水性であるため、汚泥の脱水・焼
却工程や膜分離工程のランニングコスト、イニシアルコ
ストが多大であるという点である。That is, since the sludge generation amount is extremely large at 10 to 15 kg SS / k and is difficult to dehydrate, the running cost and initial cost of the sludge dehydration / incineration process and the membrane separation process are large.
この点は、トータルプロセスとして評価する場合、重大
な欠点であり、この欠点を解決したプロセスでなければ
理想的とは言うことができない。This point is a serious drawback when evaluated as a total process, and it cannot be said to be ideal unless the process solves this drawback.
本発明は、前記従来の最新プロセスの欠点を大幅に解決
し得る新規な処理プロセスを提供することを目的として
いる。具体的には、汚泥発生量を著しく減少することに
よって、汚泥の脱水・焼却工程のランニングコスト、イ
ニシアルコストを大きく節減可能な処理プロセスを提供
するものである。It is an object of the present invention to provide a novel treatment process which can largely solve the drawbacks of the conventional state-of-the-art processes. Specifically, the present invention provides a treatment process that can significantly reduce the running cost and initial cost of the sludge dewatering / incineration process by significantly reducing the sludge generation amount.
さらに、本発明は、従来プロセスの問題点であった膜分
離工程のランニングコスト、イニシアルコストを削減す
る方式を確立することを課題としている。Another object of the present invention is to establish a method for reducing the running cost and initial cost of the membrane separation step, which are problems of the conventional process.
本発明は、し尿に高分子凝集剤を添加して凝集分離し、
該凝集分離汚泥と浄化槽汚泥を濃縮分離した濃縮汚泥の
両者を嫌気性消化したのち膜分離し、該膜透過液と前記
し尿の凝集分離機とを生物学的硝化脱窒素処理すること
を特徴とし、また、前記生物学的硝化脱窒素処理された
処理水と前記浄化槽汚泥の濃縮分離液とをさらに生物学
的硝化脱窒素処理することをも特徴とするし尿と浄化槽
汚泥の併合処理方法である。The present invention, by adding a polymer flocculant to human waste to aggregate and separate,
Both of the coagulation separation sludge and the concentrated sludge obtained by concentrating and separating the septic tank sludge are subjected to anaerobic digestion, and then membrane separation is performed, and the membrane permeate and the coagulation separator of the human waste are subjected to biological nitrification denitrification treatment. Further, the combined treatment method of human waste and septic tank sludge is characterized in that the treated water subjected to the biological nitrification denitrification treatment and the concentrated separation liquid of the septic tank sludge are further subjected to biological nitrification denitrification treatment. .
本発明の作用を、一実施態様を示す第１図を参照しなが
ら以下に説明する。The operation of the present invention will be described below with reference to FIG. 1 showing one embodiment.
毛髪、ゴム、プラスチック、紙などの粗大固形物が除去
されたし尿（除渣し尿と呼ぶ）１に、高分子凝集剤２
（カチオン系、両性のポリマー、あるいはカチオン系と
アニオン系のポリマーの併用が好適）を添加、混合し、
スクリーン、沈殿、遠心分離などの固液分離装置３によ
り生成フロックを分離し、凝集分離液４と凝集分離汚泥
５とに分ける。凝集分離汚泥５は、除渣し尿１中の微細
SS、コロイド、繊維分（セルロース系）が一体化した凝
集体となっている。Coagulant 2 for macromolecules is added to the human waste 1 from which coarse solid substances such as hair, rubber, plastics, and paper have been removed (referred to as decontamination urine).
(Cation type, amphoteric polymer, or combination of cation type and anion type polymer is suitable) is added and mixed,
The flocs produced are separated by a solid-liquid separation device 3 such as a screen, a sedimentation device, a centrifugal separation device, etc. and separated into a coagulation separation liquid 4 and a coagulation separation sludge 5. The coagulated separation sludge 5 is a fine particle in the removed urine 1.
It is an aggregate that integrates SS, colloid, and fiber (cellulose).
一方、あらかじめ粗大異物を除去した浄化槽汚泥６を、
スクリーン、沈殿、遠心分離などの固液分離装置７によ
って濃縮し、濃縮分離液８と濃縮汚泥９とに分離する。On the other hand, the septic tank sludge 6 from which coarse foreign matter has been removed in advance,
The liquid is concentrated by a solid-liquid separation device 7 such as a screen, a precipitation, a centrifugal separation, and separated into a concentrated separation liquid 8 and a concentrated sludge 9.
しかるのち、除渣し尿１の凝集分離汚泥５と浄化槽汚泥
６の濃縮汚泥９の両者を嫌気性消化槽１０に供給し、嫌
気性消化を行ったのちＵＦ膜などの膜分離装置１１で膜
分離し、膜透過液１２と膜分離消化汚泥１３とに分け
る。After that, both the coagulated separation sludge 5 of the removed urine 1 and the concentrated sludge 9 of the septic tank sludge 6 are supplied to the anaerobic digestion tank 10 and, after anaerobic digestion, membrane separation is performed by a membrane separation device 11 such as a UF membrane. Then, the membrane permeate 12 and the membrane-separated digested sludge 13 are separated.
以上の操作は、本発明の新概念の一つであり、し尿を凝
集分離して得た凝集汚泥と、一方でし尿とは別個に浄化
槽汚泥を固液分離して得た汚泥の両者を嫌気性消化し、
膜分離するという概念は類例をみない。従来は、除渣し
尿１と浄化槽汚泥６とを混合したものを、そのまま嫌気
性消化していたので、し尿中のＮＨ３−Ｎ、Ｈ２Ｓが嫌
気性消化反応を著しく阻害し、かつ大容量の消化槽を必
要としていた。The above operation is one of the new concepts of the present invention, and anaerobically both coagulated sludge obtained by coagulating separation of human waste and sludge obtained by solid-liquid separation of septic tank sludge separately from human waste. Sexually digested,
The concept of membrane separation is unique. Conventionally, a mixture of decontaminated urine 1 and septic tank sludge 6 is anaerobically digested as it is. Therefore, NH 3 -N, H 2 S in human urine significantly inhibits the anaerobic digestion reaction, and a large amount. Needed a digester tank of capacity.
しかして、除渣し尿１の凝集分離汚泥５と浄化槽汚泥６
の濃縮汚泥９を、嫌気性消化槽１０内で長時間の固形物
滞留時間（ＳＴＲ）に維持して嫌気性消化し、有機物を
ＣＨ４、ＣＯ２を主とするガスとＨ２Ｏに分解する。Then, the sludge 5 that has been decontaminated and the coagulation separation sludge 5 and the septic tank sludge 6
The concentrated sludge 9 is anaerobically digested by maintaining the solids retention time (STR) in the anaerobic digestion tank 10 for a long time, and the organic matter is decomposed into gas mainly containing CH 4 and CO 2 and H 2 O. To do.
嫌気性消化槽１０における水理滞留時間（ＨＲＴ）は１
５日以上とし、消化は高温消化でもかまわないが、常温
もしくは温度３５℃〜３７℃の中温消化が好ましく、Ｓ
ＲＴは、理想的には無限大、好ましくは１００日以上に
設定するのが良い。このような条件設定によって、凝集
分離汚泥５と濃縮汚泥９中の有機物の９０％以上が分解
され、繊維分でさえも６０％以上が分解される。これ
は、驚くべき新知見である。Hydraulic retention time (HRT) in anaerobic digester 10 is 1
The digestion may be carried out for 5 days or more, and the digestion may be carried out by high temperature digestion, but medium temperature digestion at room temperature or 35 ° C to 37 ° C is preferable.
The RT is ideally set to infinity, preferably 100 days or more. By setting such conditions, 90% or more of the organic substances in the coagulation-separation sludge 5 and the concentrated sludge 9 are decomposed, and even 60% or more of the fiber components are decomposed. This is a surprising new finding.
嫌気性消化槽１０のＳＲＴを維持する目的のうえで、後
続する消化汚泥の膜分離は極めて重要な役割を果す。膜
による固液分離は完全であり、膜透過液１２への消化汚
泥や嫌気性消化槽の流出はゼロであり、膜分離消化汚泥
１３のリサイクルによって嫌気性消化槽１０内のＳＲＴ
を極めて長く維持できるからである。１４は、極めて小
量の末消化残渣の引抜管である。For the purpose of maintaining the SRT of the anaerobic digestion tank 10, the subsequent membrane separation of digested sludge plays a very important role. The solid-liquid separation by the membrane is complete, the digestion sludge to the membrane permeate 12 and the outflow of the anaerobic digestion tank are zero, and the SRT in the anaerobic digestion tank 10 is recycled by recycling the membrane separation digestion sludge 13.
Because it can be maintained for a very long time. Reference numeral 14 is a drawing tube for an extremely small amount of undigested residue.
以上の操作により、除渣し尿１の凝集分離汚泥５と浄化
槽汚泥６の濃縮汚泥９中の有機物は、分解率９０％以上
という高度の嫌気性消化が達成される。このように有機
物が高度に分解される原因は、毒性物質であるＮＨ３−
Ｎを少なくしてあること、ＳＲＴを非常に長くすること
ができるという点のほかに、加水分解酵素、各種有機物
の可溶化菌が膜によって阻止されて系外に流出しないた
めに、セルロース、活性汚泥細胞壁などの難分解性有機
物が分解されるためと推定される。従来のし尿と浄化槽
汚泥の混合物をそのまま嫌気性消化→沈殿分離する方法
では、セルロース系繊維はほとんど分解されず、未消化
汚泥として残留してしまう。By the above operation, the organic matter in the coagulated separation sludge 5 of the removed urine 1 and the concentrated sludge 9 of the septic tank sludge 6 achieves a high degree of anaerobic digestion with a decomposition rate of 90% or more. The reason why organic matter is highly decomposed in this way is NH 3 − which is a toxic substance.
In addition to the fact that N is reduced and the SRT can be made extremely long, hydrolyzing enzymes and solubilizing bacteria of various organic substances are blocked by the membrane and do not flow out of the system. It is presumed that this is because the persistent organic substances such as sludge cell walls are decomposed. In the conventional method of anaerobic digestion → precipitation separation of the mixture of human waste and septic tank sludge as it is, the cellulosic fibers are hardly decomposed and remain as undigested sludge.
次に、除渣し尿１の凝集分離液４と嫌気性消化後の膜透
過液１２の両者を、無希釈型の生物学的硝化脱窒素工程
１５に供給し、ＢＯＤ、Ｔ−Ｎを生物学的に除去する。
しかるのち、固液分離（沈殿，遠心分離，膜分離）、好
ましくはＵＦ膜などの膜分離装置１６で膜分離し、膜透
過液１７と膜分離活性汚泥１８とに分離し、膜分離活性
汚泥１８は生物学的硝化脱窒素工程１５にリサイクルさ
れる。Next, both the aggregated separation liquid 4 of the decontaminated urine 1 and the membrane permeation liquid 12 after anaerobic digestion are supplied to the undiluted biological nitrification and denitrification step 15, and BOD and TN are biologically analyzed. To remove it.
Then, solid-liquid separation (precipitation, centrifugation, membrane separation), preferably membrane separation with a membrane separation device 16 such as a UF membrane, separates into a membrane permeate 17 and a membrane separation activated sludge 18, and the membrane separation activated sludge is obtained. 18 is recycled to the biological nitrification and denitrification step 15.
このように、本発明は、し尿中のコロイド、微細SS、繊
維分を高分子凝集剤２により高度に凝集分離し、さらに
ＳＳゼロの嫌気性消化後の膜透過液１２と共に生物学的
硝化脱窒素処理するようにプロセスを構成した結果、生
物学的硝化脱窒素工程１５には不活性ＳＳがほとんど供
給されない。従って、生物学的硝化脱窒素工程１５の活
性汚泥ＭＬＳＳには、生物反応のあずからない不活性Ｓ
Ｓ分がほとんど含まれず、この結果、生物学的硝化脱窒
素工程１５の活性汚泥ＳＲＴを長時間維持することがで
きる。このことにより余剰汚泥発生量を著しく減少でき
る。Thus, according to the present invention, colloids, fine SS, and fiber components in human waste are highly aggregated and separated by the polymer flocculant 2, and further biological nitrification and denitrification is performed with the membrane permeate 12 after anaerobic digestion with zero SS. As a result of the process being configured for nitrogen treatment, the biological nitrification denitrification step 15 is supplied with little inert SS. Therefore, in the activated sludge MLSS of the biological nitrification and denitrification step 15, inactive S that does not cause any biological reaction
Almost no S content is contained, and as a result, the activated sludge SRT in the biological nitrification and denitrification step 15 can be maintained for a long time. This can significantly reduce the amount of excess sludge generated.
１９は、ごく少量の余剰汚泥の引抜管で、引抜かれた余
剰汚泥は、直接嫌気性消化槽１０に供給するか、除渣し
尿１に混合し凝集分離すればよい。また、浄化槽汚泥６
の濃縮分離液８は、生物学的硝化脱窒素工程１５に供給
し、生物処理することができる。Reference numeral 19 is a drawing pipe for a very small amount of excess sludge, and the extracted excess sludge may be directly supplied to the anaerobic digestion tank 10 or may be removed and mixed with the urine 1 for coagulation separation. Also, septic tank sludge 6
The concentrated separated liquid 8 of can be supplied to the biological nitrification and denitrification step 15 and biologically treated.
さらに、本発明の好ましい実施態様としては、除渣し尿
１の凝集分離液４と嫌気性消化後の膜透過液１２の浄化
処理系統と、浄化槽汚泥６の濃縮分離液８の浄化処理系
を分離することである。Furthermore, as a preferred embodiment of the present invention, a purification treatment system for the coagulated separation liquid 4 of the decontaminated urine 1 and the membrane permeate 12 after anaerobic digestion and a purification treatment system for the concentrated separation liquid 8 of the septic tank sludge 6 are separated. It is to be.
即ち、除渣し尿１の凝集分離液４と凝集分離汚泥５は、
溶解性ＢＯＤ、Ｔ−Ｎなどが数１０００mg／存在する
のに対し、浄化槽汚泥６の濃縮分離液８は、溶解性ＢＯ
Ｄ、Ｔ−Ｎなどが数１０００mg／にすぎないことに着
目し、高濃度有機性汚水である凝集分離液４と嫌気性消
化後の膜透過液１２の両者のみを生物学的硝化脱窒素工
程１５に供給して生物処理したのち、膜分離装置１６で
膜分離するように構成する。一方、浄化槽汚泥６の濃縮
分離液８は、汚染度が少ないので、膜分離装置１６の膜
透過液１７に混合して第２生物学的硝化脱窒素工程２０
に供給し、生物処理を行う。That is, the coagulated separation liquid 4 and the coagulated separation sludge 5 of the removed urine 1 are
Soluble BOD, TN, etc. are present in the amount of several thousand mg /, whereas the concentrated separation liquid 8 of the septic tank sludge 6 is soluble BO.
Paying attention to the fact that D, TN, etc. are only a few 1000 mg /, both of the concentrated separation liquid 4 which is a high concentration organic wastewater and the membrane permeation liquid 12 after anaerobic digestion are subjected to a biological nitrification and denitrification process. After being supplied to 15 for biological treatment, the membrane is separated by a membrane separation device 16. On the other hand, since the concentrated separation liquid 8 of the septic tank sludge 6 has a low degree of pollution, it is mixed with the membrane permeation liquid 17 of the membrane separation device 16 and the second biological nitrification denitrification step 20.
And biological treatment.
第２生物学的硝化脱窒素工程２０の機能は、膜透過液１
７と浄化槽汚泥６の濃縮分離液８中に含まれる、少量の
ＢＯＤ、Ｔ−Ｎを生物学的に高度に除去することであ
り、第２生物学的硝化脱窒素工程２０に凝集剤２１、粉
末活性炭２２等を添加することによって、ＣＯＤ、色
度、ＰＯ▲3- 4▼をも効果的に除去することが可能であ
る。第２生物学的硝化脱窒素工程２０の生物処理水は、
さらに任意の固液分離装置２３、好ましくは膜分離装置
で固液分離され、高度処理水２４として流出する。The function of the second biological nitrification and denitrification step 20 is that the membrane permeate 1
7 and biologically highly removing a small amount of BOD and TN contained in the concentrated separated liquid 8 of the septic tank sludge 6, and the coagulant 21 in the second biological nitrification and denitrification step 20. It is possible to effectively remove COD, chromaticity, and PO - 3-4 by adding powdered activated carbon 22 and the like. The biologically treated water of the second biological nitrification denitrification step 20 is
Further, it is subjected to solid-liquid separation in any solid-liquid separation device 23, preferably a membrane separation device, and flows out as highly treated water 24.
なお、第２生物学的硝化脱窒素工程２０への流入液中に
場内雑排水２５を混合し、同時に生物処理することもで
きる。It is also possible to mix the wastewater 25 in the site with the inflow liquid to the second biological nitrification denitrification step 20 and simultaneously perform biological treatment.
このように、第２生物学的硝化脱窒素工程２０を利用す
ることにより、無希釈の生物学的硝化脱窒素工程１５
が、浄化槽汚泥６の流入によって希釈されないため、生
物酸化熱による温度上昇を高く維持することができ、水
量負荷も少なくなるから小容量の設備で効率良い硝化脱
窒素処理が可能になる。さらに、活性汚泥の膜分離装置
１６への水量負荷も少なくなり、膜の所要面積と動力コ
ストが減小するという大きな利点が得られる。Thus, by using the second biological nitrification / denitrification step 20, the undiluted biological nitrification / denitrification step 15
However, since it is not diluted by the inflow of the septic tank sludge 6, it is possible to maintain a high temperature rise due to the heat of biological oxidation and reduce the load of water amount, so that it is possible to perform an efficient nitrification denitrification process with a small-capacity facility. Further, the load of water amount of the activated sludge on the membrane separation device 16 is reduced, and a large advantage is obtained that the required area of the membrane and the power cost are reduced.
以下に本発明の実施例を示す。 Examples of the present invention will be shown below.
し尿中の夾雑物、繊維分を微細目スクリーンで除去した
のち、カチオン系ポリマー（エバグロースＣ１０４Ｇ、
商品名）を２５０mg／添加し、３０秒攪拌した結果、
強い大きなフロックが形成され、目開き１mmの傾斜型ウ
ェッジワイヤスクリーンで容易にフロックが分離でき
た。この分離された汚泥（凝集分離汚泥）の固形物濃度
は、4.3％と高濃度であった。After removing impurities and fibers in human waste with a fine mesh screen, a cationic polymer (Ebagrose C104G,
250 mg / brand name) was added and the result of stirring for 30 seconds
A strong and large flock was formed, and the slanted wedge wire screen with an opening of 1 mm could easily separate the flock. The solid content of the separated sludge (coagulated separation sludge) was as high as 4.3%.
一方、浄化槽汚泥を遠心濃縮機により濃縮分離した濃縮
汚泥の固形物濃度は、4.2％となった。On the other hand, the solid concentration of the sludge obtained by concentrating and separating the septic tank sludge by the centrifugal concentrator was 4.2%.
次に、前記のし尿の凝集分離汚泥と浄化槽汚泥の濃縮汚
泥の混合汚泥（重量比１：１）を、温度３５℃の嫌気性
消化槽（槽内攪拌は機械的に行った）に供給し、ＨＲＴ
を１５日間に設定し、汚泥の酸発酵、可溶化、及びメタ
ン発酵を進行させた。Next, the mixed sludge (weight ratio 1: 1) of the above-mentioned coagulation separation sludge of night soil and concentrated sludge of septic tank sludge was supplied to an anaerobic digestion tank at a temperature of 35 ° C (the stirring inside the tank was mechanically performed). , HRT
Was set for 15 days, and sludge acid fermentation, solubilization, and methane fermentation were allowed to proceed.
嫌気性消化槽から流出する消化汚泥をＵＦ膜により完全
に膜分離し、膜分離消化汚泥を嫌気性消化槽にリサイク
ルした。また、この膜透過液と前記の傾斜型ウェッジワ
イヤスクリーンで分離されたし尿の凝集分離液とを混合
し、生物学的硝化脱窒素工程に供給した。The digested sludge flowing out from the anaerobic digester was completely separated by UF membrane, and the membrane-separated digested sludge was recycled to the anaerobic digester. Further, this membrane-permeated liquid was mixed with the aggregated separated liquid of night soil separated by the inclined wedge wire screen and supplied to the biological nitrification and denitrification step.
なお、嫌気性消化汚泥はＵＦ膜により完全に分離されて
リサイクルされ、系外には全く流出しないため、嫌気性
消化槽のＳＲＴを２００日以上に設定可能であり、この
結果、汚泥中有機物の約90％が分解し、未消化残渣は1.
2kg／ｋと極めて少量であった。Since the anaerobic digestion sludge is completely separated by the UF membrane and recycled, and does not flow out of the system at all, the SRT of the anaerobic digestion tank can be set to 200 days or more. About 90% is decomposed and the undigested residue is 1.
It was an extremely small amount of 2 kg / k.
前記生物学的硝化脱窒素工程に供給された嫌気性消化膜
分離液とし尿の凝集分離液の混合液の水質は表−１に示
す通りであった。The water quality of the mixed liquid of the anaerobic digestive membrane separation liquid and the urine aggregation separation liquid supplied to the biological nitrification and denitrification step was as shown in Table 1.
生物学的硝化脱窒素工程の運転条件を表−２に示す。 Table 2 shows the operating conditions for the biological nitrification and denitrification process.
表−２の生物学的硝化脱窒素工程のＵＦ膜透過液の水質
は表−３に示す通りであった。 The water quality of the UF membrane permeate in the biological nitrification and denitrification step in Table 2 was as shown in Table 3.
また、浄化槽汚泥の濃縮分離液は、前記ＵＦ膜透過液と
共に硫酸バンド１５００mg／，粉末活性炭６００mg／
を添加して、第２生物学的硝化脱窒素工程及び膜分離
工程（中空糸膜）にて処理した。その処理水水質を表−
４に示す。 Further, the concentrated separation liquid of the septic tank sludge is, together with the UF membrane permeation liquid, a sulfuric acid band of 1500 mg /, a powdered activated carbon of 600 mg /
Was added and treated in the second biological nitrification and denitrification step and the membrane separation step (hollow fiber membrane). The treated water quality is shown in the table −
4 shows.
なお、生物学的硝化脱窒素工程の６ケ月間の連続実験
中、余剰汚泥の引抜きは不要であった。この原因は、流
入液の不活性ＳＳ分がほとくどなく、活性汚泥のＭＬＳ
Ｓも高濃度であるため、余剰汚泥の発生量が非常に少な
いためと考えられる。 It should be noted that during the 6-month continuous experiment of the biological nitrification and denitrification process, it was not necessary to withdraw excess sludge. The reason for this is that the inactive SS content of the influent is very small and MLS of activated sludge is
It is considered that since S also has a high concentration, the amount of excess sludge generated is very small.
以上述べたように、本発明によれば次のような卓越した
効果を奏する。As described above, the present invention has the following outstanding effects.
従来プロセスに比べ、汚泥発生量が著しく少なくな
り、膜分離、脱水、焼却等の汚泥処理工程が大幅に合理
化される。Compared with the conventional process, the amount of sludge generated is significantly reduced, and the sludge treatment processes such as membrane separation, dehydration and incineration are greatly streamlined.
生物学的硝化脱窒素工程から余剰活性汚泥がほとんど
発生しない。Almost no excess activated sludge is generated from the biological nitrification and denitrification process.
し尿と浄化槽汚泥を直接嫌気性消化するのではなく、
し尿の凝集分離汚泥と浄化槽汚泥の濃縮汚泥の混合物を
嫌気性消化→膜分離するようにした結果、し尿の液側に
高濃度に存在する嫌気性消化阻害物質（ＮＨ３−Ｎ、Ｈ
２Ｓ）が嫌気性消化槽に流入しない。このため、極めて
効果的な嫌気性消化反応が進み、汚泥中の有機物が徹底
的に分解される。Instead of directly anaerobically digesting human waste and septic tank sludge,
As a result of anaerobic digestion → membrane separation of a mixture of coagulated separation sludge of human waste and concentrated sludge of septic tank sludge, an anaerobic digestion inhibitor (NH 3 -N, H) present at a high concentration on the liquid side of human waste.
2 S) does not flow into the anaerobic digester. Therefore, an extremely effective anaerobic digestion reaction proceeds, and organic matter in sludge is thoroughly decomposed.
第１図は本発明の一実施態様を示す系統説明図である。 １……し尿、２……高分子凝集剤、３，７，２３……固
液分離装置、４……凝集分離液、５……凝集分離汚泥、
６……浄化槽汚泥、８……濃縮分離液、９……濃縮汚
泥、１０……嫌気性消化槽、１１，１６……膜分離装
置、１２，１７……膜透過液、１３……膜分離消化汚
泥、１５……生物学的硝化脱窒素工程、１８……膜分離
活性汚泥、２０……第２生物学的硝化脱窒素工程、２１
……凝集剤、２２……粉末活性炭、２４……高度処理
水。FIG. 1 is a system diagram showing an embodiment of the present invention. 1 ... human waste, 2 ... polymer flocculant, 3,7,23 ... solid-liquid separation device, 4 ... coagulation separation liquid, 5 ... coagulation separation sludge,
6 ... septic tank sludge, 8 ... concentrated separation liquid, 9 ... concentrated sludge, 10 ... anaerobic digestion tank, 11, 16 ... membrane separation device, 12, 17 ... membrane permeate, 13 ... membrane separation Digested sludge, 15 …… Biological nitrification and denitrification process, 18 …… Membrane separation activated sludge, 20 …… Second biological nitrification and denitrification process, 21
…… Coagulant, 22 …… Powdered activated carbon, 24 …… Highly treated water.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.5 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０２Ｆ 3/28 ＺＡＢ Ｚ 3/34 ＺＡＢ １０１ Ａ 11/04 ＺＡＢ Ｚ 7824−4Ｄ 11/12 ＺＡＢ Ｅ 7824−4Ｄ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 5 Identification code Office reference number FI Technical display location C02F 3/28 ZAB Z 3/34 ZAB 101 A 11/04 ZAB Z 7824-4D 11/12 ZAB E 7824-4D
Claims (2)
し、該凝集分離汚泥と浄化槽汚泥を濃縮分離した濃縮汚
泥の両者を嫌気性消化したのち膜分離し、該膜透過液と
前記し尿の凝集分離液とを生物学的硝化脱窒素処理する
ことを特徴とするし尿と浄化槽汚泥の併合処理方法。1. A high molecular coagulant is added to human waste to coagulate and separate, and both the coagulated and separated sludge and the concentrated sludge obtained by concentrating and separating the septic tank sludge are subjected to anaerobic digestion and then membrane separated, and the membrane permeate and the above A combined treatment method of human waste and septic tank sludge, which comprises subjecting the aggregated separated liquid of human waste to biological nitrification and denitrification.
と前記浄化槽汚泥の濃縮分離液とをさらに生物学的硝化
脱窒素処理するものである請求項１記載のし尿と浄化槽
汚泥の併合処理方法。2. The combined use of human waste and septic tank sludge according to claim 1, wherein the treated water subjected to the biological nitrification denitrification treatment and the concentrated separation liquid of the septic tank sludge are further subjected to biological nitrification denitrification treatment. Processing method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25005490A JPH0647119B2 (en) | 1990-09-21 | 1990-09-21 | Combined treatment method of human waste and septic tank sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25005490A JPH0647119B2 (en) | 1990-09-21 | 1990-09-21 | Combined treatment method of human waste and septic tank sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04131199A JPH04131199A (en) | 1992-05-01 |
| JPH0647119B2 true JPH0647119B2 (en) | 1994-06-22 |
Family
ID=17202118
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25005490A Expired - Lifetime JPH0647119B2 (en) | 1990-09-21 | 1990-09-21 | Combined treatment method of human waste and septic tank sludge |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0647119B2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2796909B2 (en) * | 1992-07-27 | 1998-09-10 | 株式会社荏原総合研究所 | Wastewater treatment method |
| JP3442288B2 (en) * | 1998-07-06 | 2003-09-02 | 株式会社クボタ | Methane fermentation method for organic waste |
| JP4605877B2 (en) * | 2000-09-21 | 2011-01-05 | 前澤工業株式会社 | Flock particle size control method and water treatment method |
| JP2002336825A (en) * | 2001-05-17 | 2002-11-26 | Kubota Corp | Method for recycling organic waste |
| JP5371510B2 (en) * | 2009-03-27 | 2013-12-18 | 大阪瓦斯株式会社 | Combined treatment of wastewater and organic residue |
| JP5867796B2 (en) * | 2011-03-30 | 2016-02-24 | 株式会社クボタ | Waste water treatment method and waste water treatment system |
| JP5242739B2 (en) * | 2011-05-23 | 2013-07-24 | 三菱重工環境・化学エンジニアリング株式会社 | Methane fermentation post-treatment device, methane fermentation post-treatment system, and methods thereof |
-
1990
- 1990-09-21 JP JP25005490A patent/JPH0647119B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH04131199A (en) | 1992-05-01 |
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