JPH0694040B2 - Water purification method and device - Google Patents
Water purification method and deviceInfo
- Publication number
- JPH0694040B2 JPH0694040B2 JP3268681A JP26868191A JPH0694040B2 JP H0694040 B2 JPH0694040 B2 JP H0694040B2 JP 3268681 A JP3268681 A JP 3268681A JP 26868191 A JP26868191 A JP 26868191A JP H0694040 B2 JPH0694040 B2 JP H0694040B2
- Authority
- JP
- Japan
- Prior art keywords
- treatment
- slurry
- unit
- biological
- section
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 46
- 238000000034 method Methods 0.000 title claims description 33
- 238000000746 purification Methods 0.000 title claims description 5
- 238000011282 treatment Methods 0.000 claims description 100
- 239000002002 slurry Substances 0.000 claims description 43
- 238000003756 stirring Methods 0.000 claims description 31
- 238000004062 sedimentation Methods 0.000 claims description 23
- 239000000463 material Substances 0.000 claims description 17
- 230000001737 promoting effect Effects 0.000 claims description 16
- 244000005700 microbiome Species 0.000 claims description 12
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 230000001112 coagulating effect Effects 0.000 claims description 7
- 238000005345 coagulation Methods 0.000 claims description 6
- 230000015271 coagulation Effects 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 238000013019 agitation Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 2
- 230000004931 aggregating effect Effects 0.000 claims 1
- 230000001376 precipitating effect Effects 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 40
- 239000000126 substance Substances 0.000 description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000000460 chlorine Substances 0.000 description 7
- 229910052801 chlorine Inorganic materials 0.000 description 7
- 239000000701 coagulant Substances 0.000 description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 150000004045 organic chlorine compounds Chemical class 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000009287 sand filtration Methods 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229920001661 Chitosan Polymers 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 230000001629 suppression Effects 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000004071 biological effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- CBXWGGFGZDVPNV-UHFFFAOYSA-N so4-so4 Chemical compound OS(O)(=O)=O.OS(O)(=O)=O CBXWGGFGZDVPNV-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000002636 symptomatic treatment Methods 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 239000013076 target substance Substances 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
Landscapes
- Biological Treatment Of Waste Water (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、水中の懸濁物質、アン
モニア性窒素、ＢＯＤ成分、臭気物質などを効率良く除
去する方法およびその装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for efficiently removing suspended substances in water, ammoniacal nitrogen, BOD components, odorous substances and the like.
【０００２】[0002]
【従来の技術】上水道において最も普及している通常の
処理方法は、前塩素凝集沈殿ろ過処理であり、次のフロ
ーからなる。 原水 → 前塩素 → 凝集沈殿 → 砂ろ過 → 後
塩素 → 浄水 しかしながら、近年の水源の富栄養化の進行に伴う水質
の悪化、カビ臭の発生、および水中の有機物と塩素の反
応によって生成するトリハロメタン等の有機塩素化合物
の問題は、上記の通常の処理では対応しきれないケース
も生じており、より高度な処理方法が必要となってきて
いる。これが、いわゆる高度処理で、オゾン処理、活性
炭処理、ＢＡＣ（生物活性炭）処理、生物酸化処理など
がある。オゾン処理は、オゾンの持つ強力な酸化力を利
用して、原水中の有機物、カビ臭、色度などを除去する
もので、特にカビ臭に対して優れた効果を有するがアン
モニア性窒素は除去できない。有機塩素化合物の生成抑
制に関しては、原水中の有機物質の性状によって効果の
ある場合とない場合があるといわれる。また、オゾン処
理は上記の通常の処理フローにおいて砂ろ過の後段に設
置されるが、現在はオゾン処理の後には必ず活性炭処理
を必要とし、イニシアルコストが高いのが問題点であ
る。活性炭処理には粉末活性炭法と粒状活性炭法があ
る。処理の対象は何れも原水中の有機物、カビ臭物質な
どであるが、粒状活性炭法が活性炭の再生使用を行う恒
久的な施設を前提としているのに対し、粉末活性炭法は
カビ臭発生時などにのみ使用する使い捨ての対症療法的
な処理である点が異なる。粉末活性炭法は上記の通常の
処理フローにおいて前塩素の前段に適用されるが、この
場合、前塩素は粉末活性炭により消失する。定常的な処
理を要する場合には粒状活性炭処理の方がコスト的に有
利であり、砂ろ過の後段に設置される。活性炭処理は非
常に優れた処理方式であるが、処理寿命が短く、処理コ
ストが高いのが最大の問題点である。ＢＡＣ処理はオゾ
ン＋活性炭の処理で、処理寿命の短い活性炭処理の前段
でオゾン処理を行うことにより、活性炭の処理寿命を長
くしようというものである。これはオゾン処理によって
後段の活性炭処理の負荷を軽減すると共に、原水中の難
生物分解性有機物質を生物が利用できる形態に変化さ
せ、活性炭に吸着された有機物の生物分解機能を高める
ことができるためと説明されている。上記の通常の処理
フローにおいて、砂ろ過の前、あるいは後に設置する案
などが検討されている。ＢＡＣ処理は、高度処理の中で
最高級の処理であるが、コストが高いのと広大な設置面
積を要するのが問題点である。生物酸化処理は各種媒体
に微生物を担持させ、その代謝を利用して有機物質等を
除去するもので、使用する媒体によってハニカムチュー
ブ法、回転円板法、固定床式粒状媒体法、流動床式粒状
媒体法などがある。この処理法は原水中のアンモニア性
窒素、ＢＯＤ成分、カビ臭物質、および還元性物質を対
象としたもので、運転管理に高度の技術を要せず、上記
の通常の処理フローにおいて、主として前塩素の前段に
設置される。2. Description of the Related Art The most popular general treatment method in waterworks is pre-chlorine coagulation sedimentation filtration treatment, which comprises the following flows. Raw water → Pre-chlorine → Coagulation sedimentation → Sand filtration → Post-chlorine → Purified water However, water quality has deteriorated due to the progress of eutrophication of water sources in recent years, mold odor is generated, and trihalomethane generated by the reaction of chlorine with organic matter in water In some cases, the problem of the organic chlorine compound cannot be dealt with by the above-mentioned ordinary treatment, and a more advanced treatment method is required. This is a so-called advanced treatment, which includes ozone treatment, activated carbon treatment, BAC (biological activated carbon) treatment, biological oxidation treatment, and the like. Ozone treatment removes organic substances, mold odor, chromaticity, etc. in raw water by utilizing the strong oxidizing power of ozone. It has an excellent effect on mold odor, but removes ammoniacal nitrogen. Can not. It is said that the suppression of the production of organic chlorine compounds may or may not be effective depending on the properties of organic substances in raw water. Further, the ozone treatment is installed in the latter stage of the sand filtration in the above-mentioned ordinary treatment flow, but at present, the activated carbon treatment is always required after the ozone treatment, and there is a problem that the initial cost is high. The activated carbon treatment includes a powdered activated carbon method and a granular activated carbon method. The target of the treatment is organic matter in the raw water, musty odorous substances, etc., whereas the granular activated carbon method presupposes a permanent facility for reusing the activated carbon, whereas the powdered activated carbon method gives a musty odor. The only difference is that it is a disposable symptomatic treatment that is only used for. The powdered activated carbon method is applied to the preceding stage of pre-chlorine in the above-mentioned ordinary processing flow, but in this case, pre-chlorine is eliminated by the powdered activated carbon. When constant treatment is required, granular activated carbon treatment is more cost effective and is installed after sand filtration. Activated carbon treatment is a very excellent treatment method, but the biggest problems are short treatment life and high treatment cost. The BAC treatment is a treatment of ozone + activated carbon, and is intended to extend the treatment life of activated carbon by performing the ozone treatment before the activated carbon treatment having a short treatment life. This reduces the load of activated carbon treatment in the latter stage by ozone treatment, changes the biodegradable organic substances in raw water into a form that can be used by living organisms, and enhances the biodegradation function of organic substances adsorbed on activated carbon. It is explained as a reason. In the above normal processing flow, a plan to install before or after sand filtration is being considered. BAC processing is the highest-class processing among advanced processing, but its problems are high cost and a large installation area. Biological oxidation treatment is to remove microorganisms such as organic substances by supporting microorganisms in various media.The honeycomb tube method, rotating disk method, fixed bed type granular media method, fluidized bed method is used depending on the medium used. There is a granular medium method. This treatment method is intended for ammonia nitrogen, BOD components, musty odor substances, and reducing substances in raw water, and does not require high technology for operation management. It is installed before chlorine.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、運転管理に
高度の技術を要せず、水中のアンモニア性窒素、ＢＯＤ
成分、カビ臭物質および還元性物質の除去を行う生物酸
化処理を採用するものであるが、従来の生物酸化処理で
は生物濃度をあまり大きくできないため高濃度のカビ臭
には対応しきれず、生物活性の低下する低水温時にはア
ンモニア性窒素の硝化能力が著しく低下するなどの問題
が生じ、また、上水道水源などでは、生物分解できる有
機塩素化合物前駆物質が元々があまり多くないため、汚
染の進んだ水源では有機塩素化合物生成抑制の面でも対
応できない場合も起こっていた。さらに、従来の生物酸
化処理の場合、通常の処理設備以外に広大な設置面積が
必要であることも用地確保の面で問題であった。本発明
は、生物酸化処理の上記問題点を解決すべく、生物酸化
処理のリアクターと凝集沈殿設備を一体化させて生物濃
度を高め、処理効果を著しく向上させる浄水処理方法お
よびその装置を提供することを目的とするものである。DISCLOSURE OF THE INVENTION The present invention does not require a high level of technical skill for operation management, and does not require ammonia nitrogen in water or BOD.
It adopts a biooxidation treatment that removes components, musty odor substances and reducing substances.However, conventional biooxidation treatment cannot increase the biological concentration so much that it cannot cope with a high concentration of musty odor. When the water temperature is low, there is a problem that the nitrification capacity of ammonia nitrogen is significantly reduced.In addition, there are not many organic chlorine compound precursors that can be biodegraded in tap water sources. Then, there were cases where it was not possible to cope with the suppression of the formation of organic chlorine compounds. Further, in the case of the conventional biological oxidation treatment, it is also a problem from the viewpoint of securing the site that a vast installation area is required in addition to the usual treatment equipment. In order to solve the above-mentioned problems of biooxidation treatment, the present invention provides a water purification treatment method and an apparatus thereof, which integrates a biooxidation treatment reactor and a coagulation-sedimentation facility to increase the organism concentration and remarkably improve the treatment effect. That is the purpose.
【０００４】[0004]
【課題を解決するための手段】本発明は、凝集剤等の混
合を行う急速攪拌部、フロック形成を行う緩速攪拌部お
よびフロック沈殿部にて凝集沈殿処理するに際し、微生
物の担体となる生物処理促進材を投入すると共に、前記
フロック沈殿部で濃縮されたスラリーおよび生物処理促
進材の混合物の全部もしくは一部を前記急速攪拌部もし
くは緩速攪拌部に循環返送し、スラリー中の微生物濃度
を高めて生物酸化処理と凝集沈殿処理を同時に行うこと
を特徴とする浄水処理方法であり、また、凝集剤等の混
合を行う急速攪拌部、フロック形成を行う緩速攪拌部お
よびフロック沈殿部を備え、該フロック沈殿部で濃縮さ
れたスラリーの全部もしくは一部を前記急速攪拌部もし
くは緩速攪拌部へ循環返送するように構成したスラリー
循環型凝集沈殿装置に、微生物の担体となる生物処理促
進材投入部を設けたことを特徴とする浄水処理装置であ
る。MEANS FOR SOLVING THE PROBLEMS The present invention provides an organism that serves as a carrier for microorganisms in the flocculation and precipitation treatment in a rapid stirring section for mixing a flocculant and the like, a slow stirring section for floc formation and a floc precipitation section. With the addition of the processing accelerator, the whole or a part of the mixture of the slurry and the biological treatment accelerator concentrated in the floc precipitation section is circulated back to the rapid stirring section or the slow stirring section, and the concentration of microorganisms in the slurry is adjusted. It is a purified water treatment method characterized by simultaneously performing bio-oxidation treatment and coagulation sedimentation treatment at the same time, and also comprises a rapid agitation unit for mixing flocculants, a slow agitation unit for floc formation and a floc sedimentation unit. A slurry circulation-type coagulating sedimentation device configured to circulate and return all or part of the slurry concentrated in the floc sedimentation unit to the rapid stirring unit or the slow stirring unit. To a water treatment apparatus characterized in that a biological treatment promoting material supplying portion serving as carrier microorganisms.
【０００５】[0005]
【作用】本発明では、アルミニウム塩、鉄塩などを代表
とする無機凝集剤による、もしくはこれらの無機凝集剤
と無機および有機の凝集助剤等の組合せによる凝集沈殿
処理方法において、原水中、あるいは凝集剤等の混合を
行う急速攪拌部、フロック形成を行う緩速攪拌部等に微
生物の担体となる生物処理促進材を所定の濃度となるよ
うに投入し、その後は沈殿スラリーの引き抜きにより失
われる量に見合った量が補給され、一定濃度に保たれ
る。生物処理促進材としては、材質、形状、大きさなど
については特に限定するものではなく、微生物が付着す
るものならば何でもよく、単一物質でも複数物質でもか
まわないが、植物、動植物の化石、石油、合成樹脂など
を原料とする粒状，粉状の活性炭、炭あるいはそれらを
主成分とした造粒物やキトサンビーズが好ましい。そし
て、通水に伴い、生物処理促進材には各種分解菌、硝化
細菌等が高濃度に繁殖して生物酸化処理能力が高まり、
原水中のアンモニア性窒素、ＢＯＤ成分、臭気物質など
は高レベルに分解される。また、スラリー濃度を一定の
レベルに保持するために適宜スラリーが引き抜かれる
が、スラリーと共に引き抜かれ量に見合った量の生物処
理促進材が補給される。引き抜かれたスラリー中の生物
処理促進材は、回収、再使用するのが好ましく、このス
ラリーを回収槽へ導き、凝集剤フロックと生物処理促進
材の比重差を利用した分離方法、ｐＨ値調整による凝集
剤フロックの溶解を利用した分離方法などによる生物処
理促進材の回収を行えば、この生物処理促進材を再使用
することができ極めて経済的となる。また、回収した生
物処理促進材に対して加熱再生、水蒸気再生、薬液再生
などの賦活再生を実施してから再利用する方法を取るこ
ともできる。In the present invention, in the coagulation-sedimentation treatment method using an inorganic coagulant typified by an aluminum salt, an iron salt or the like, or a combination of these inorganic coagulant and an inorganic or organic coagulant aid, raw water, or A biological treatment accelerator, which is a carrier of microorganisms, is added to a rapid stirring section for mixing a flocculant and the like, a slow stirring section for forming flocs to a predetermined concentration, and thereafter, it is lost by withdrawing the precipitated slurry. It is replenished in an amount commensurate with the amount and kept at a constant concentration. The biological treatment promoting material is not particularly limited in terms of material, shape, size, etc., as long as microorganisms adhere to it, it may be a single substance or multiple substances, plants, fossils of plants and animals, Granular or powdered activated carbon made of petroleum, synthetic resin or the like, charcoal, granules containing them as a main component or chitosan beads are preferable. Then, along with the passage of water, various degrading bacteria, nitrifying bacteria, etc. propagate in the biological treatment promoting material at high concentrations, and the biological oxidation treatment capacity increases,
Ammonia nitrogen, BOD components, odorous substances, etc. in raw water are decomposed to a high level. Further, the slurry is appropriately withdrawn in order to maintain the slurry concentration at a constant level, but an amount of the biological treatment accelerator corresponding to the amount withdrawn is replenished together with the slurry. It is preferable to collect and reuse the biological treatment promoting material in the extracted slurry, and to introduce this slurry into a recovery tank to separate the flocculant flocs and the biological processing promoting material using a separation method by adjusting the pH value. If the biological treatment promoting material is recovered by a separation method utilizing dissolution of flocculant floc, the biological treatment promoting material can be reused, which is extremely economical. Further, it is also possible to adopt a method in which the recovered biological treatment promoting material is subjected to activation regeneration such as heating regeneration, steam regeneration, chemical solution regeneration, and the like, and then reused.
【０００６】本発明の最大の利点でもある一つ目の特長
は、生物酸化処理と凝集沈殿処理を一体化させたことに
ある。このことにより、前記の通常の浄水処理を実施し
ている施設であって、高度処理導入を必要としている施
設にあっては、既設の凝集沈殿処理設備を本発明による
高度処理設備に改造すること、もしくは既設の凝集沈殿
処理設備の敷地を利用して本発明による高度処理設備を
新設することが可能であり、高度処理設備設置のための
新たな用地の確保が不要となり、高度処理導入のための
経済的負担が極めて軽減される。なお、本発明は他の高
度処理との併用を妨げるものではないから、本発明によ
る高度処理設備の前段もしくは後段に、オゾン処理、活
性炭処理、ＢＡＣ処理などの処理を組合せることも可能
である。この場合、本発明単独の処理よりもさらに効率
的な、さらに高度の処理が実施できるのは勿論のこと、
併設する他の高度処理設備への負荷を軽減できるため、
その設備ならびに用地を小さくすることが可能となる。
本発明の特長の二つ目は、処理フローの中で生物処理
促進材を凝集フロック・スラリーとともに循環させるこ
とにより、生物濃度を高めたことである。本発明の実施
形態としては、スラリー循環型の高速凝集沈殿設備のよ
うにスラリー濃度を任意に調整可能なものが最適である
が、沈殿部からの濃縮スラリーを攪拌部へ循環返送する
機構を設けた横流式沈殿設備のような形態も可能であ
る。なお、上水道の原水においては、元々ＢＯＤが低
く、かつ溶存酸素も飽和に近い形で含まれ、生物処理プ
ロセスで必要とされる酸素を既に保持している場合が殆
どであるため、エアレーションなどによる酸素供給は本
発明の実施にあたっての必ずしも必須要件とならない場
合が多いが、酸素供給を行った方が生物処理上有利とな
ることは言うまでもない。また、原水中のアンモニア性
窒素、カビ臭物質、還元性物質などの生物処理対象物質
濃度が高く、原水の溶存酸素だけでは酸素が不足する場
合には、酸素供給を行うことが望ましい。これらの場合
の酸素供給方法についても特に限定するものではない
が、原水流入部もしくは急速攪拌部などに対しエアレー
ションする方法が最適である。また、生物処理促進材の
回収再利用を行う際に、回収後の生物処理促進材に対し
て水中でエアレーションを行い、生物活性を高めた上で
再利用することなども有効な方法である。The first advantage, which is the greatest advantage of the present invention, is that the bio-oxidation treatment and the coagulation-sedimentation treatment are integrated. Due to this, in the facility that is performing the above-mentioned normal water purification treatment and that requires the introduction of advanced treatment, the existing coagulation-sedimentation treatment facility should be converted to the advanced treatment facility according to the present invention. Alternatively, it is possible to newly install the advanced treatment equipment according to the present invention by using the existing site of the coagulation sedimentation treatment equipment, and it is not necessary to secure a new site for installing the advanced treatment equipment. The economic burden of is greatly reduced. Since the present invention does not prevent the combined use with other advanced treatments, it is also possible to combine treatments such as ozone treatment, activated carbon treatment, BAC treatment, etc., before or after the advanced treatment equipment according to the present invention. . In this case, it is of course possible to carry out a more advanced process, which is more efficient than the process of the present invention alone,
Since it can reduce the load on other advanced processing equipment attached to the facility,
It is possible to reduce the equipment and the site.
The second feature of the present invention is that the biological concentration is increased by circulating the biological treatment promoting material together with the floc slurry in the treatment flow. As an embodiment of the present invention, a slurry circulation type high-speed coagulation-sedimentation facility that can arbitrarily adjust the slurry concentration is optimal, but a mechanism for circulating and returning the concentrated slurry from the precipitation section to the stirring section is provided. A configuration such as a cross-flow type precipitation facility is also possible. Originally, the raw water of water supply has a low BOD and also contains dissolved oxygen in a form close to saturation, and in most cases it already holds oxygen required for biological treatment processes. In many cases, oxygen supply is not always an essential requirement for carrying out the present invention, but it goes without saying that oxygen supply is advantageous in biological treatment. Further, when the concentration of the biological treatment target substance such as ammoniacal nitrogen, musty odor substance, reducing substance, etc. in the raw water is high and oxygen is insufficient only by the dissolved oxygen in the raw water, it is desirable to supply oxygen. The oxygen supply method in these cases is also not particularly limited, but the method of aerating the raw water inflow section or the rapid stirring section is optimal. Further, when collecting and reusing the biological treatment promoting material, it is also an effective method to aerate the recovered biological treatment promoting material in water to enhance the biological activity and then reuse.
【０００７】[0007]
【実施例】本発明の一実施例を、スラリー循環型高速凝
集沈殿装置の設備を例にとり図面をもって説明すると、
以下のとおりである。図１において、原水流入管１は槽
内中央部の急速攪拌室２内に開口しており、急速攪拌室
２には凝集剤注入管３が開口すると共に中央上部はイン
ペラ５を介して緩速攪拌室６に連なり、緩速攪拌室６の
上部は外周のスラリー分離部７に連なり、スラリー分離
部７の下部はスラリー濃縮部４を介して急速攪拌室２の
下部に連なっている。８はスラリー分離部７の上部の集
水部である。さらに、微生物の担体となる生物処理促進
材投入部１０が原水流入管１に設けられるが、直接槽内
の適宜の箇所に設けることもできる。しかして、原水は
原水流入管１を通って急速攪拌室２に流入するが、急速
攪拌室２には凝集剤３が注入されるとともに、外周に位
置するスラリー濃縮部４より一部が循環返送スラリーと
して返送されており、急速攪拌室２中央上部に配された
インペラ５により良く攪拌混合される。次いで、インペ
ラ５の側面より上部の緩速攪拌室６に導かれ、緩速攪拌
効果によって凝集フロックが形成された後、外周に位置
するスラリー分離部７において処理水とスラリーに分離
され、処理水は集水部８を通って後段に送られる。ここ
で、生物処理促進材は運転開始時に所定の濃度となるよ
うに原水又は槽内へ一括投入、もしくは所定の濃度とな
るまで運転中に投入するなどの方式で凝集スラリー内に
均一に分散されており、その後は沈殿スラリーの引き抜
きにより失われる量に見合った量が適宜急速攪拌室２へ
添加補給され、一定濃度に保たれる。通水に伴い、生物
処理促進材には原水中のカビ臭物質分解菌、アンモニア
硝化菌などが高濃度に繁殖してスラリーの生物酸化処理
能力が高まり、原水中のカビ臭物質、アンモニア性窒
素、ＢＯＤ成分などは急速攪拌室２、緩速攪拌室６、ス
ラリー分離部７でのスラリーとの接触を通し、高レベル
に分解される。また、スラリー濃度を一定レベルに保持
するためにスラリー濃縮部４より適宜引き抜かれたスラ
リーは、生物処理促進材回収槽９送られ、生物処理促進
材が回収、再利用できる。EXAMPLE An example of the present invention will be described with reference to the drawings by taking the equipment of a slurry circulation type high-speed coagulating sedimentation device as an example.
It is as follows. In FIG. 1, a raw water inflow pipe 1 is opened in a rapid stirring chamber 2 in the center of the tank, a coagulant injection pipe 3 is opened in the rapid stirring chamber 2, and an upper part of the center is slowed through an impeller 5. It is connected to the stirring chamber 6, the upper part of the slow stirring chamber 6 is connected to the slurry separating section 7 on the outer periphery, and the lower part of the slurry separating section 7 is connected to the lower part of the rapid stirring chamber 2 via the slurry concentrating section 4. Reference numeral 8 is a water collecting section above the slurry separating section 7. Further, although the biological treatment promoting material charging unit 10 serving as a carrier for microorganisms is provided in the raw water inflow pipe 1, it may be directly provided in an appropriate place in the tank. Then, although the raw water flows into the rapid stirring chamber 2 through the raw water inflow pipe 1, the flocculant 3 is injected into the rapid stirring chamber 2, and a part of the raw water is circulated and returned from the slurry concentrating section 4 located on the outer periphery. It is returned as a slurry and is well agitated and mixed by the impeller 5 arranged in the upper center of the rapid agitation chamber 2. Then, after being introduced from the side surface of the impeller 5 into the slow stirring chamber 6 and forming flocs of flocs by the slow stirring effect, the slurry is separated into the treated water and the slurry in the slurry separating section 7 located on the outer periphery. Is sent to the latter stage through the water collecting section 8. Here, the biological treatment promoting material is uniformly dispersed in the agglomerated slurry by a method such as batch injection into raw water or a tank so as to have a predetermined concentration at the start of operation, or addition during operation until a predetermined concentration is reached. After that, an amount commensurate with the amount lost due to the withdrawal of the precipitated slurry is appropriately added and replenished to the rapid stirring chamber 2 to maintain a constant concentration. Along with water flow, biodegradation bacteria, mold odor-decomposing bacteria in raw water, ammonia nitrifying bacteria, etc. breed in high concentrations and the bio-oxidizing ability of the slurry increases, and mold odor substances in raw water, ammoniacal nitrogen , BOD components, etc. are decomposed to a high level through contact with the slurry in the rapid stirring chamber 2, the slow stirring chamber 6, and the slurry separating unit 7. Further, the slurry appropriately extracted from the slurry concentrating unit 4 in order to keep the slurry concentration at a constant level is sent to the biological treatment promoting material recovery tank 9 so that the biological treatment promoting material can be recovered and reused.
【０００８】次に実験例を示す実験例１ 平均内径１０ｍｍのハニカムチューブを用いた、処理水
量１００ｍ3/日のハニカムチューブ式生物処理装置とス
ラリー循環型凝集沈殿装置の組合せによる従来法と、生
物処理促進材とスラリー循環型凝集沈殿装置を用いた本
発明法のアンモニア性窒素除去性能の比較を表１に示
す。両者共に凝集剤として硫酸ばん土を２０〜３０mg/l
急速攪拌部に添加し、本発明ではさらに生物処理促進材
として１〜３mmφのキトサンビーズを２００mg/l投入し
た。従来法の場合水温の低下する１２月以降のアンモニ
ア性窒素除去率が極端に低下したが、本発明法では良好
な処理が行われていた。 Experimental Example 1 showing an experimental example: A conventional method using a combination of a honeycomb tube type biological treatment apparatus and a slurry circulation type coagulating sedimentation apparatus using a honeycomb tube having an average inner diameter of 10 mm and a treated water amount of 100 m 3 / day. Table 1 shows a comparison of the ammoniacal nitrogen removal performance of the method of the present invention using a treatment accelerator and a slurry circulation type coagulating sedimentation apparatus. Both of them use 20-30 mg / l of sulphate sulfate as a coagulant.
It was added to the rapid stirring section, and in the present invention, 200 mg / l of 1 to 3 mmφ chitosan beads was further added as a biological treatment accelerator. In the case of the conventional method, the ammonia nitrogen removal rate was drastically decreased after December when the water temperature decreased, but the method of the present invention performed a good treatment.
【０００９】[0009]
【表１】 [Table 1]
【００１０】実験例２ 平均内径１０ｍｍのハニカムチューブを用いた、処理水
量１００ｍ3/日のハニカムチューブ式生物処理装置とス
ラリー循環型凝集沈殿装置の組合せによる従来法と、生
物処理促進材とスラリー循環型凝集沈殿装置を用いた本
発明法のカビ臭物質除去性能の比較を表２に示す。表２
の通り従来法では除去能が低下する時においても、本発
明法は安定した高い除去能を示した。なお、凝集剤及び
生物処理促進材は実験例１と同様である。 Experimental Example 2 Using a honeycomb tube having an average inner diameter of 10 mm, a treatment method of 100 m 3 / day and a combination of a honeycomb tube type biological treatment apparatus and a slurry circulation type coagulating sedimentation apparatus, a biological treatment accelerator and slurry circulation. Table 2 shows a comparison of the musty odor substance removing performance of the method of the present invention using a type coagulating sedimentation device. Table 2
As described above, the method of the present invention showed stable and high removal ability even when the removal ability was lowered by the conventional method. The coagulant and the biological treatment accelerator are the same as in Experimental Example 1.
【００１１】[0011]
【表２】 [Table 2]
【００１２】[0012]
【発明の効果】以上述べたように、本発明によれば、微
生物濃度を高めた生物酸化処理と凝集沈殿処理とを同時
に行い、水中のアンモニア性窒素、ＢＯＤ成分、臭気物
質を高度に除去すると共に懸濁物質も除去し、既設設備
の利用を容易に可能にするものである。As described above, according to the present invention, the biological oxidation treatment with an increased concentration of microorganisms and the coagulation sedimentation treatment are simultaneously performed to highly remove ammonia nitrogen, BOD components and odorous substances in water. At the same time, suspended solids are also removed, making it easy to use existing equipment.
【図１】本発明の一実施例に使用されるスラリー循環型
高速凝集沈殿装置の縦断面図である。FIG. 1 is a vertical cross-sectional view of a slurry circulation type high-speed coagulation-sedimentation apparatus used in an embodiment of the present invention.
【符号の説明】 １ 原水流入管 ２ 急速攪拌室 ３ 凝集剤注入管 ４ スラリー濃縮部 ５ インペラ ６ 緩速攪拌室 ７ スラリー分離部 ８ 集水部 ９ 生物処理促進材回収槽 10 生物処理促進材投入部[Explanation of symbols] 1 raw water inflow pipe 2 rapid stirring chamber 3 coagulant injection pipe 4 slurry concentration unit 5 impeller 6 slow speed stirring chamber 7 slurry separation unit 8 water collection unit 9 biological treatment accelerator recovery tank 10 biological treatment accelerator input Department
Claims (2)
ック形成を行う緩速攪拌部およびフロック沈殿部にて凝
集沈殿処理するに際し、微生物の担体となる生物処理促
進材を投入すると共に、前記フロック沈殿部で濃縮され
たスラリーおよび生物処理促進材の混合物の全部もしく
は一部を前記急速攪拌部もしくは緩速攪拌部に循環返送
し、スラリー中の微生物濃度を高めて生物酸化処理と凝
集沈殿処理を同時に行うことを特徴とする浄水処理方
法。1. At the time of aggregating and precipitating in a rapid agitation unit for mixing a flocculant and the like, a slow agitation unit for floc formation, and a floc sedimentation unit, a biological treatment accelerator that serves as a carrier for microorganisms is added, All or part of the mixture of the slurry and the biological treatment accelerator concentrated in the floc settling section is circulated back to the rapid stirring section or the slow stirring section to increase the concentration of microorganisms in the slurry to perform biological oxidation treatment and coagulation precipitation. A water purification method characterized in that the treatments are carried out simultaneously.
ック形成を行う緩速攪拌部およびフロック沈殿部を備
え、該フロック沈殿部で濃縮されたスラリーの全部もし
くは一部を前記急速攪拌部もしくは緩速攪拌部へ循環返
送するように構成したスラリー循環型凝集沈殿装置に、
微生物の担体となる生物処理促進材投入部を設けたこと
を特徴とする浄水処理装置。2. A rapid stirring unit for mixing a flocculant, etc., a slow stirring unit for forming flocs, and a floc sedimentation unit, wherein all or part of the slurry concentrated in the floc sedimentation unit is the rapid stirring unit. Alternatively, a slurry circulation type coagulating sedimentation device configured to circulate back to the slow stirring unit,
A water purification device characterized by comprising a biological treatment promoting material charging section that serves as a carrier for microorganisms.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3268681A JPH0694040B2 (en) | 1991-09-20 | 1991-09-20 | Water purification method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3268681A JPH0694040B2 (en) | 1991-09-20 | 1991-09-20 | Water purification method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0576897A JPH0576897A (en) | 1993-03-30 |
| JPH0694040B2 true JPH0694040B2 (en) | 1994-11-24 |
Family
ID=17461919
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3268681A Expired - Lifetime JPH0694040B2 (en) | 1991-09-20 | 1991-09-20 | Water purification method and device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0694040B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010079118A (en) * | 2001-06-15 | 2001-08-22 | 백운국 | sludge circulation type rapid clarifier |
| JP3773169B2 (en) * | 2001-06-29 | 2006-05-10 | 株式会社荏原製作所 | High speed biological treatment method and apparatus for organic wastewater |
| JP4933473B2 (en) * | 2008-03-31 | 2012-05-16 | 水ｉｎｇ株式会社 | Slurry circulation type coagulation sedimentation treatment apparatus and operation method thereof |
| JP5173538B2 (en) * | 2008-04-03 | 2013-04-03 | 水ｉｎｇ株式会社 | Water treatment method |
| JP5753702B2 (en) * | 2011-02-23 | 2015-07-22 | 水ｉｎｇ株式会社 | Formation method of initial mother floc in high speed coagulation sedimentation basin |
-
1991
- 1991-09-20 JP JP3268681A patent/JPH0694040B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0576897A (en) | 1993-03-30 |
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