JP2008237958A - Sewage treatment method and apparatus - Google Patents
Sewage treatment method and apparatus Download PDFInfo
- Publication number
- JP2008237958A JP2008237958A JP2007078058A JP2007078058A JP2008237958A JP 2008237958 A JP2008237958 A JP 2008237958A JP 2007078058 A JP2007078058 A JP 2007078058A JP 2007078058 A JP2007078058 A JP 2007078058A JP 2008237958 A JP2008237958 A JP 2008237958A
- Authority
- JP
- Japan
- Prior art keywords
- sewage
- reaction tank
- liquid
- biological reaction
- amount
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000010865 sewage Substances 0.000 title claims abstract description 131
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000010802 sludge Substances 0.000 claims abstract description 196
- 238000006243 chemical reaction Methods 0.000 claims abstract description 145
- 239000007788 liquid Substances 0.000 claims abstract description 144
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 238000004062 sedimentation Methods 0.000 claims description 111
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 110
- 239000012141 concentrate Substances 0.000 claims description 20
- 238000001556 precipitation Methods 0.000 claims description 2
- 239000002562 thickening agent Substances 0.000 abstract 4
- 230000002265 prevention Effects 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000012528 membrane Substances 0.000 description 11
- 244000005700 microbiome Species 0.000 description 9
- 230000001771 impaired effect Effects 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000006228 supernatant Substances 0.000 description 5
- 238000001914 filtration Methods 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- IXPNQXFRVYWDDI-UHFFFAOYSA-N 1-methyl-2,4-dioxo-1,3-diazinane-5-carboximidamide Chemical compound CN1CC(C(N)=N)C(=O)NC1=O IXPNQXFRVYWDDI-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 241001453382 Nitrosomonadales Species 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- ZGOFOSYUUXVFEO-UHFFFAOYSA-N [Fe+4].[O-][Si]([O-])([O-])[O-] Chemical compound [Fe+4].[O-][Si]([O-])([O-])[O-] ZGOFOSYUUXVFEO-UHFFFAOYSA-N 0.000 description 1
- 229920006317 cationic polymer Polymers 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 235000010413 sodium alginate Nutrition 0.000 description 1
- 229940005550 sodium alginate Drugs 0.000 description 1
- 239000000661 sodium alginate Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 239000002351 wastewater 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
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
本発明は、下水を生物反応を用いて処理する下水処理方法及び下水処理装置に関する。 The present invention relates to a sewage treatment method and a sewage treatment apparatus for treating sewage using a biological reaction.
一般的な下水処理装置は、例えは、図３に示すように、生物反応槽１と最終沈殿池２とを備えており、生物反応槽１にて、まず、生物反応を利用して主として有機物や、ＢＯＤや、窒素分等を除去し、その後、最終沈殿池２にて、生物反応により生じたフロック等を沈降分離して分離液を河川や海に放流している。このような下水処理装置の処理能力は、主として生物反応槽１での処理能力に基づいて決定しており、通常、晴天時における最大流入水量を基準として設計流入水量を決定し、下水処理が行われている。 For example, as shown in FIG. 3, a general sewage treatment apparatus includes a biological reaction tank 1 and a final sedimentation basin 2. In the biological reaction tank 1, first, organic substances are mainly utilized using a biological reaction. In addition, BOD, nitrogen content, and the like are removed, and then, in the final sedimentation basin 2, flocs and the like generated by biological reactions are settled and discharged into rivers and the sea. The treatment capacity of such a sewage treatment apparatus is determined mainly based on the treatment capacity in the biological reaction tank 1, and usually the design inflow water amount is determined on the basis of the maximum inflow water amount in fine weather, and the sewage treatment is performed. It has been broken.
しかしながら、汚水と雨水を遮集する合流式下水道の下水処理装置では、雨天時に下水処理装置に流入する下水量が急増し、処理に供せられる下水量が、設計流入水量を超過してしまう。 However, in the combined sewer sewage treatment apparatus that collects sewage and rainwater, the amount of sewage flowing into the sewage treatment apparatus during rainy weather increases rapidly, and the amount of sewage provided for the treatment exceeds the design inflow water amount.
そこで、雨天時下水の水質は、雨水により希釈化されていることから、そのまま放流してもあまり問題を生じることが少ないという事情により、従来は、雨水時の増水分の下水を、生物反応槽１にて処理することなく、そのまま放流もしくは薬剤などで消毒して放流している。 Therefore, since the quality of sewage in rainy weather is diluted with rainwater, it has been difficult to cause problems even if it is discharged as it is. Without being treated in step 1, it is discharged as it is or sterilized with chemicals or the like.
また、汚水のみを遮集する分流式下水道の下水処理においても、雨天時に浸入水等の影響で、流入下水が設計流入水量を超過する場合があり、その設計流入水量を超えた水量については、そのまま放流もしくは薬剤などで消毒して放流が行われている。 In addition, even in sewerage sewerage systems that intercept only sewage, inflow sewage may exceed the design inflow due to intrusion water during rainy weather. It is released as it is or sterilized with chemicals.
また、下記特許文献１には、合流式下水道において下水流入量が計画最大流入量に対して一定割合の超過量を超えない場合には、流入下水の全量を最初沈殿池、生物反応槽、最終沈殿池で二次処理まで行い、さらに、ろ材を充填したろ過槽に流入させて処理する一方、下水流入量が計画最大流入量に対して一定割合の超過量を超えた場合には、計画最大流入量に対して一定割合の超過量分の流入下水については前記二次処理まで行い放流するとともに、計画最大流入量に対して一定割合の超過量を超えた量の流入下水については最初沈殿池で一次処理した後にろ過槽へ流入させて処理するか、最初沈殿池を通さずにきょう雑物を除去した後にろ過槽へ流入させて処理することが開示されている。 Further, in Patent Document 1 below, if the sewage inflow does not exceed a certain percentage of the planned maximum inflow in the combined sewer system, the total amount of inflow sewage is set as the initial sedimentation tank, biological reaction tank, The secondary treatment is performed in the settling basin, and further processed by flowing into a filtration tank filled with filter media. On the other hand, if the sewage inflow exceeds a certain maximum with respect to the planned maximum inflow, the maximum The inflowing sewage with a certain percentage of the inflow is discharged up to the above-mentioned secondary treatment, and the inflowing sewage exceeding the certain percentage of the planned maximum inflow is the first sedimentation basin. It is disclosed that the first treatment is performed after flowing into the filtration tank, or the impurities are removed without first passing through the settling basin and then the flow is introduced into the filtration tank.
また、下記特許文献２には、雨天時に増量した流入下水の少なくとも一部を導入して分離水と凝集分離汚泥に分離する凝集分離装置と、前記分離水を放流する配管と、前記流入下水の一部を導入して分離水と沈殿汚泥に分離する最初沈殿池と、前記最初沈殿池からの分離水と該凝集分離装置からの凝集沈殿汚泥とを導入して脱リンする嫌気部、脱窒部、又は好気部を有する嫌気好気式生物脱リン設備と、前記脱リン設備からの汚泥を含有する被脱リン水を導入して分離液と沈殿汚泥に分離する最終沈殿池とを有する下水処理装置が開示されている。 Further, in Patent Document 2 below, a flocculating / separating device that introduces at least a part of the inflowing sewage increased in the rain to separate it into separated water and flocculated separation sludge, a pipe for discharging the separated water, and the inflowing sewage A first settling basin where a part is introduced and separated into separated water and settling sludge; an anaerobic portion for dephosphorization by introducing the separated water from the first settling basin and the settling sludge from the coagulation separation device; and denitrification Or anaerobic and aerobic biological dephosphorization equipment having an aerobic part, and a final sedimentation basin for introducing dephosphorized water containing sludge from the dephosphorization equipment and separating it into a separation liquid and a precipitated sludge A sewage treatment apparatus is disclosed.
また、下記特許文献３には、下水を沈殿処理した後、その上澄水を生物処理部で生物処理し、その処理液を分離液と汚泥とに固液分離し、分離汚泥の一部を生物処理部の入口側に返送する下水処理方法において、該生物処理部として、嫌気処理用の前段生物処理部と、好気処理用の後段生物処理部とが設けられており、該上澄水の流量が所定流量以下のときには、前記上澄水の全量を該前段生物処理部と後段生物処理部とにこの順で流通させ、該上澄水の流量が該所定流量を超えるときには、該上澄水の一部を該前段生物処理部と後段生物処理部とにこの順で流通させ、該上澄水の残部は前段生物処理部を経ることなく後段生物処理部に流入させて処理することが開示されている。
下水の水質によっては、雨天時の増水によって希釈化されているとはいえ、有機物や、ＢＯＤや、窒素分等が、放流限界値を超過している場合がある。このため、上記特許文献１、２のように、これらを何ら除去することなく河川や海などに放流した場合、放流先である河川や海などの水質に影響が生じるおそれがあった。 Depending on the quality of the sewage, organic matter, BOD, nitrogen, etc. may exceed the discharge limit value even though it is diluted by water increase during rainy weather. For this reason, as described in Patent Documents 1 and 2, when the water is discharged into a river or the sea without removing them, the water quality of the river or the sea as a discharge destination may be affected.
一方、上記特許文献３では、設計流入水量を超過する場合であっても、生物反応槽にその全量を投入して生物処理する方法を行っている。しかしながら、生物反応槽に設計流入水量を超えた水量を流入させると、生物反応槽内の汚泥濃度が希釈されて処理能力が低下するので、有機物や、ＢＯＤや、窒素分等が十分低減されないまま放流されるおそれがあった。更には、最終沈殿池に設計流入水量を超える処理液を供給して沈降分離しているので、沈殿池の滞留時間に影響して、汚泥の沈降が不十分となり、分離液に汚泥が流出することがあり、下水処理が破綻するおそれがあった。 On the other hand, in the above-mentioned Patent Document 3, even when the design inflow water amount is exceeded, a biological treatment method is performed by introducing the entire amount into the biological reaction tank. However, if the amount of water in excess of the design inflow water amount is allowed to flow into the biological reaction tank, the sludge concentration in the biological reaction tank is diluted and the processing capacity is lowered, so that organic matter, BOD, nitrogen content, etc. are not sufficiently reduced. There was a risk of being released. Furthermore, since the treatment liquid exceeding the design inflow water amount is supplied to the final sedimentation basin and the sedimentation is separated, the sludge sedimentation is insufficient due to the residence time of the sedimentation basin, and the sludge flows into the separation liquid. In some cases, the sewage treatment may fail.
したがって、本発明の目的は、雨天時の増水等によって、処理の対象となる下水の流入量が設計流入水量を超過した場合であっても、下水を効率よく処理することができ、更には、汚泥の流出を防止できる水処理方法及び水処理装置を提供することである。 Therefore, an object of the present invention is to treat sewage efficiently even when the inflow amount of sewage to be treated exceeds the design inflow amount due to water increase during rainy weather, etc. It is providing the water treatment method and water treatment apparatus which can prevent the outflow of sludge.
上記目的を達成するため、本発明の下水処理方法は、下水を生物反応槽で生物処理し、その処理液を最終沈殿池で分離液と汚泥とに沈降分離する下水処理方法において、前記生物反応槽への下水の流入水量が設計流入水量以下の場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池で沈降分離し、前記生物反応槽への下水の流入水量が設計流入水量を超える場合、流入下水の全量を前記生物反応槽で生物処理した後、設計流入水量の処理液を前記最終沈殿池で沈降分離すると共に、設計流入水量を超過した水量の処理液を、前記最終沈殿槽に導入する前に活性汚泥濃縮装置に供給して分離液と活性汚泥濃縮液とに濃縮分離し、この活性汚泥濃縮液を前記生物反応槽に返送することを特徴とする。 In order to achieve the above object, the sewage treatment method of the present invention is a sewage treatment method in which sewage is biologically treated in a biological reaction tank, and the treated liquid is settled and separated into a separation liquid and sludge in a final sedimentation basin. If the inflow of sewage into the tank is less than the designed inflow, the entire amount of inflow sewage is biologically treated in the biological reaction tank, and then the entire amount of the treated liquid is settled and separated in the final sedimentation basin. If the inflow of sewage exceeds the design inflow, the total amount of inflow sewage was biologically treated in the biological reaction tank, and then the design inflow was treated and settled in the final sedimentation basin, and the design inflow was exceeded. Before introducing the treatment liquid of the amount of water into the activated sludge concentrator before introducing it into the final sedimentation tank, the separated liquid and the activated sludge concentrated liquid are concentrated and separated, and the activated sludge concentrated liquid is returned to the biological reaction tank. It is characterized by.
本発明の下水処理方法によれば、下水を生物反応槽１に供して生物反応処理すると共に、設計流入水量を超過した水量の処理液を活性汚泥濃縮装置に送って濃縮分離し、活性汚泥濃縮液を生物反応槽に返送する構成としているので、生物反応槽への下水の流入水量が設計流入水量を超過した場合であっても、生物反応槽内の活性汚泥の濃度が低下しにくく、ほぼ一定濃度を維持できるので、生物反応槽における下水の処理効率が損なわれにくい。そして、最終沈殿池には、設計量を超えた処理液は導入されないので、最終沈殿池から排出される分離液には汚泥が流出しにくく、放流先の河川や海などへの影響が小さい。 According to the sewage treatment method of the present invention, the sewage is supplied to the biological reaction tank 1 for biological reaction treatment, and the treatment liquid having an amount of water that exceeds the design inflow water amount is sent to the activated sludge concentrator to concentrate and separate the activated sludge. Since the liquid is returned to the biological reaction tank, even if the amount of sewage inflow into the biological reaction tank exceeds the designed inflow, the concentration of activated sludge in the biological reaction tank is unlikely to decrease. Since a constant concentration can be maintained, the treatment efficiency of sewage in the biological reaction tank is not easily impaired. And since the processing liquid exceeding the design amount is not introduced into the final sedimentation basin, the sludge hardly flows out into the separation liquid discharged from the final sedimentation basin, and the influence on the discharge destination river or sea is small.
本発明の下水処理方法のもう一つは、下水を生物反応槽で生物処理し、その処理液を最終沈殿池で分離液と汚泥とに沈降分離する下水処理方法において、前記生物反応槽への下水の流入水量が設計流入水量以下の場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池で沈降分離し、前記生物反応槽への下水の流入水量が設計流入水量を超える場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池に供給し、その後前記最終沈殿池から設計流入水量を超過した水量の処理液を取り出して活性汚泥濃縮装置に供給し、分離液と活性汚泥濃縮液とに濃縮分離して、この活性汚泥濃縮液を前記生物反応槽に返送すると共に、前記残った処理液を、前記最終沈殿池で沈降分離することを特徴とする。 Another sewage treatment method of the present invention is a sewage treatment method in which sewage is biologically treated in a biological reaction tank, and the treated liquid is settled and separated into a separation liquid and sludge in a final sedimentation basin. If the inflow of sewage is less than or equal to the design inflow, the entire amount of inflow sewage is biologically treated in the biological reaction tank, and then the entire amount of the treated liquid is settled and separated in the final sedimentation basin, and the inflow of sewage into the biological reaction tank When the amount of water exceeds the design inflow water amount, the entire amount of influent sewage is biologically treated in the biological reaction tank, and then the entire amount of the treated liquid is supplied to the final sedimentation basin, and then the amount of water that exceeds the design inflow water amount from the final sedimentation basin. Is taken out and supplied to the activated sludge concentrating device, concentrated and separated into a separated liquid and an activated sludge concentrated liquid, the activated sludge concentrated liquid is returned to the biological reaction tank, and the remaining treated liquid is Settling and separating in the final settling tank It is characterized in.
この態様によれば、下水を生物反応槽に供して生物反応処理すると共に、生物反応槽での超過水量分を含む処理液を一旦最終沈殿池に導入し、その後、最終沈殿池から超過水量分の処理液を取り出して活性汚泥濃縮装置へ送り濃縮分離し、活性汚泥濃縮液を生物反応槽に返送するようにしているので、生物反応槽への下水の流入水量が増えても、生物反応槽内の活性汚泥の濃度が低下しにくく、ほぼ一定濃度を維持できるので、生物反応槽における下水の処理効率が損なわれにくい。また、活性汚泥濃縮装置へ供給される処理液は、最終沈殿池に導入した際に、多少なりとも処理が行われているので、活性汚泥濃縮装置の負荷を低減できる。 According to this aspect, the sewage is supplied to the biological reaction tank for biological reaction treatment, and the treatment liquid containing the excess water amount in the biological reaction tank is once introduced into the final sedimentation basin, and then the excess water amount from the final sedimentation basin. The treatment liquid is taken out, sent to the activated sludge concentrator, concentrated and separated, and the activated sludge concentrate is returned to the biological reaction tank, so even if the inflow of sewage into the biological reaction tank increases, the biological reaction tank Since the concentration of the activated sludge in the inside is difficult to decrease and a substantially constant concentration can be maintained, the treatment efficiency of the sewage in the biological reaction tank is hardly impaired. Further, since the treatment liquid supplied to the activated sludge concentrator is treated to some extent when introduced into the final sedimentation basin, the load on the activated sludge concentrator can be reduced.
また、本発明の下水処理装置は、下水を生物処理する生物反応槽と、生物処理後の処理液を分離液と汚泥に分離処理する最終沈殿池と、生物処理後の処理液を分離液と活性汚泥濃縮液に濃縮分離する活性汚泥濃縮装置と、前記生物反応槽から前記最終沈殿池に処理液を通水させる第１の通水経路と、設計流入水量を超過した水量の処理液を、前記生物反応槽から活性汚泥濃縮装置に通水させる第２の通水経路と、前記最終沈殿池から前記生物反応槽に前記汚泥を返送させる第１の返送経路と、前記活性汚泥濃縮装置から前記生物反応槽に前記活性汚泥濃縮液を返送させる第２の返送経路とを備えることを特徴とする。 Further, the sewage treatment apparatus of the present invention includes a biological reaction tank for biologically treating sewage, a final sedimentation basin for separating the biologically treated treatment liquid into a separated liquid and sludge, and a biologically treated treatment liquid as a separated liquid. An activated sludge concentrator that concentrates and separates into an activated sludge concentrate, a first water passage that allows the treatment liquid to flow from the biological reaction tank to the final sedimentation basin, and a treatment liquid having an amount of water that exceeds the design inflow water amount, From the biological reaction tank to the activated sludge concentrating device, the second water passage route, from the final sedimentation basin to the biological reaction vessel to return the sludge to the biological reaction tank, from the activated sludge concentrating device And a second return path for returning the activated sludge concentrate to the biological reaction tank.
本発明の下水処理装置によれば、流入下水の全量が生物反応槽で処理された後、設計流入水量を超過した水量の処理液は、第２の通水経路から活性汚泥濃縮装置に導入されて濃縮分離されるので、最終沈殿池には設計量を超過する水量の処理液は導入されない。このため、最終沈殿池での処理効率は損なわれにくく、分離液中に汚泥が極めて流出しにくい。また、活性汚泥濃縮装置に導入された処理液は濃縮分離され、活性汚泥濃縮液は生物反応槽に返送されるので、生物反応槽の汚泥濃度は低下しにくく、生物反応槽での処理効率は損なわれにくい。 According to the sewage treatment apparatus of the present invention, after the entire amount of inflow sewage is treated in the biological reaction tank, the treatment liquid having an amount of water exceeding the design inflow water amount is introduced into the activated sludge concentrating device from the second water passage. Therefore, the final settling basin is not introduced with a treatment solution with an amount of water exceeding the design amount. For this reason, the processing efficiency in the final sedimentation basin is not easily impaired, and sludge hardly flows out into the separated liquid. In addition, since the treatment liquid introduced into the activated sludge concentrator is concentrated and separated and the activated sludge concentrate is returned to the biological reaction tank, the sludge concentration in the biological reaction tank is unlikely to decrease, and the treatment efficiency in the biological reaction tank is Hard to be damaged.
本発明の下水処理装置のもう一つは、下水を生物処理する生物反応槽と、生物処理後の処理液を分離液と汚泥に分離処理する最終沈殿池と、生物処理後の処理液を分離液と活性汚泥濃縮液に濃縮分離する活性汚泥濃縮装置と、前記生物反応槽から前記最終沈殿池に処理液を通水させる第１の通水経路と、設計流入水量を超過した水量の処理液を前記最終沈殿池から活性汚泥濃縮装置に通水させる第２の通水経路と、前記最終沈殿池から前記生物反応槽に前記汚泥を返送させる第１の返送経路と、前記活性汚泥濃縮装置から前記生物反応槽に前記活性汚泥濃縮液を返送させる第２の返送経路とを備えることを特徴とする。 Another sewage treatment apparatus of the present invention separates a biological reaction tank that biologically treats sewage, a final sedimentation basin that separates the biological treatment liquid into a separation liquid and sludge, and a biological treatment liquid. Activated sludge concentrating device for concentration and separation into a liquid and an activated sludge concentrate, a first water flow path for passing the treatment liquid from the biological reaction tank to the final sedimentation basin, and a treatment liquid having an amount of water exceeding the design inflow water quantity From the final sedimentation basin to the activated sludge concentrating device, from the final sedimentation basin to the biological reaction tank, the first return passage, and from the activated sludge concentrating device. And a second return path for returning the activated sludge concentrate to the biological reaction tank.
この態様によれば、流入下水の全量が生物反応槽で処理された後、超過水量分を含む処理液の全量を一旦最終沈殿池に導入し、その後、最終沈殿池から超過水量分の処理液を取り出して活性汚泥濃縮装置へ送り、活性汚泥濃縮液を生物反応槽に返送するようにしているので、生物反応槽への下水の流入水量が設計流入水量を超過した場合であっても、生物反応槽内の活性汚泥の濃度が低下しにくく、生物反応槽での処理効率が損なわれにくい。また、活性汚泥濃縮装置へ供給される処理液は、最終沈殿池に導入された際に、多少なりとも処理が行われているので、活性汚泥濃縮装置の負荷は低減される。 According to this aspect, after the entire amount of influent sewage is treated in the biological reaction tank, the entire amount of the treatment liquid including the excess water amount is once introduced into the final sedimentation basin, and then the treatment liquid for the excess water amount from the final sedimentation basin. Is taken out and sent to the activated sludge concentrator and the activated sludge concentrate is returned to the biological reaction tank, so even if the amount of sewage inflow into the biological reaction tank exceeds the designed inflow, The concentration of activated sludge in the reaction tank is unlikely to decrease, and the processing efficiency in the biological reaction tank is unlikely to be impaired. Moreover, since the process liquid supplied to the activated sludge concentrator is processed to some extent when it is introduced into the final sedimentation basin, the load on the activated sludge concentrator is reduced.
本発明によれば、下水を生物反応槽に供して生物反応処理すると共に、設計流入水量を超過した水量の処理液を活性汚泥濃縮装置に送って濃縮分離し、活性汚泥濃縮液を生物反応槽に返送するようにしているので、生物反応槽への下水の流入量が増えても、生物反応槽内の活性汚泥の濃度が低下しにくく、ほぼ一定濃度を維持できるので、生物反応槽における下水の処理効率が損なわれにくい。そして、最終沈殿池では、設計流入水量以下の処理液を沈降分離するので、最終沈殿池には過剰汚泥が蓄積されにくく、また、最終沈殿池から排出される分離液には汚泥が流出しにくいので、放流先の河川や海などへの影響が小さい。 According to the present invention, sewage is supplied to a biological reaction tank for biological reaction treatment, and a treatment liquid having an amount exceeding the design inflow water amount is sent to the activated sludge concentrator to concentrate and separate, and the activated sludge concentrate is converted into the biological reaction tank. Therefore, even if the amount of sewage inflow into the bioreactor increases, the concentration of activated sludge in the bioreactor is less likely to decrease and can be maintained at a substantially constant concentration. The processing efficiency is difficult to be impaired. In the final sedimentation basin, the treatment liquid below the design inflow water amount is settled and separated, so that excess sludge is unlikely to accumulate in the final sedimentation basin, and sludge does not easily flow out into the separation liquid discharged from the final sedimentation basin. Therefore, the impact on the river or the sea of the discharge destination is small.
以下、本発明について図面を用いて更に詳細に説明する。図１は、本発明の下水処理装置の第１の実施形態の概略構成図である。 Hereinafter, the present invention will be described in more detail with reference to the drawings. FIG. 1 is a schematic configuration diagram of a first embodiment of a sewage treatment apparatus of the present invention.
この下水処理装置は、生物反応槽１と、最終沈殿池２と、活性汚泥濃縮装置３とで構成されている。 This sewage treatment apparatus is composed of a biological reaction tank 1, a final sedimentation basin 2, and an activated sludge concentration apparatus 3.
生物反応槽１は、槽内に微生物を含む活性汚泥が滞留し、微生物の作用によって下水を脱窒処理、脱リン処理できる処理槽であれば特に限定はなく、例えば、アンモニア酸化菌や亜硝酸酸化菌などの好気性微生物を含む曝気槽、亜硝酸酸化菌などの好気性微生物と脱窒菌などの嫌気性微生物を含む間欠曝気槽などを用いることができる。 The biological reaction tank 1 is not particularly limited as long as activated sludge containing microorganisms stays in the tank and can denitrify and dephosphorize sewage by the action of microorganisms. For example, ammonia oxidizing bacteria and nitrous acid can be used. An aeration tank containing aerobic microorganisms such as oxidizing bacteria, an intermittent aeration tank containing aerobic microorganisms such as nitrite oxidizing bacteria and anaerobic microorganisms such as denitrifying bacteria, and the like can be used.
この生物反応槽１には、図示しない最初沈殿池等の下水供給源から伸びた配管Ｌ１と、最終沈殿池２から伸びた配管Ｌ２と、活性汚泥濃縮装置３から伸びた配管Ｌ３とが接続している。 The biological reaction tank 1 is connected to a pipe L1 extending from a sewage supply source such as a first sedimentation tank (not shown), a pipe L2 extending from the final sedimentation tank 2, and a pipe L3 extending from the activated sludge concentrator 3. ing.
生物反応槽１からは、配管Ｌ４が伸びて、最終沈殿池２に接続している。また、生物反応槽１からは、配管Ｌ５が伸びて活性汚泥濃縮装置３に接続しており、設計流入水量を超過した水量の処理液を、配管Ｌ５から活性汚泥濃縮装置３に導入できるように構成されている。 A pipe L4 extends from the biological reaction tank 1 and is connected to the final sedimentation tank 2. Moreover, from the biological reaction tank 1, the pipe L5 is extended and connected to the activated sludge concentrating device 3, so that the treatment liquid having an amount of water exceeding the design inflow water amount can be introduced into the activated sludge concentrating device 3 from the pipe L5. It is configured.
最終沈殿池２は、導入された処理水を分離液と汚泥とに沈降分離できる処理槽であれば特に限定ない。そして、最終沈殿池２から、配管Ｌ６が伸びて、沈降分離後の分離液を系外に放流できるように構成されている。また、最終沈殿池２からは、配管Ｌ２と、配管Ｌ７とが伸びて、沈降分離後の汚泥を系外に引き抜くことができるように構成されている。 The final sedimentation basin 2 is not particularly limited as long as it is a treatment tank capable of settling and separating the introduced treated water into a separation liquid and sludge. And the piping L6 is extended from the final sedimentation basin 2, and it is comprised so that the separation liquid after sedimentation separation can be discharged out of the system. Moreover, from the final sedimentation tank 2, the piping L2 and the piping L7 are extended, and it is comprised so that the sludge after sedimentation can be extracted out of the system.
活性汚泥濃縮装置３は、導入された処理液を、分離液と活性汚泥濃縮液とに濃縮分離できる処理装置であれば特に限定はなく、例えば、精密ろ過膜（ＭＦ膜）、限外ろ過膜（ＵＦ膜）、ナノろ過膜（ＮＦ膜）等のろ過膜を備えた、中空糸膜モジュール、平膜型モジュール、スパイラル型モジュール、管型モジュール等の形態の膜モジュールが挙げられる。そして、活性汚泥濃縮装置３からは配管Ｌ８が伸びて、濃縮分離後の分離液を系外に放流できるように構成されている。また、活性汚泥濃縮装置３からは、配管Ｌ３が伸びて、濃縮分離後の活性汚泥濃縮液を系外に引き抜くことができるように構成されている。 The activated sludge concentrating device 3 is not particularly limited as long as it is a processing device capable of concentrating and separating the introduced processing liquid into a separated liquid and an activated sludge concentrated liquid. For example, a microfiltration membrane (MF membrane), an ultrafiltration membrane is used. Examples of the membrane module include a hollow fiber membrane module, a flat membrane type module, a spiral type module, and a tube type module, which are provided with a filtration membrane such as (UF membrane) and nanofiltration membrane (NF membrane). And the piping L8 is extended from the activated sludge concentration apparatus 3, and it is comprised so that the separation liquid after concentration separation can be discharged out of the system. Moreover, from the activated sludge concentrating device 3, the pipe L3 extends so that the activated sludge concentrated liquid after concentration and separation can be drawn out of the system.
次に、この下水処理装置を用いた本発明の下水処理方法について説明する。 Next, the sewage treatment method of the present invention using this sewage treatment apparatus will be described.
生物反応槽１への下水の流入水量が設計流入水量以下の場合においては、配管Ｌ１から流入された下水が、生物反応槽１にて槽内の微生物の作用によって、脱窒処理、脱リン処理されて、有機物、窒素成分、リン成分が低減ないし除去される。 When the amount of sewage inflow into the biological reaction tank 1 is less than or equal to the design inflow water, the sewage flowing in from the pipe L1 is denitrified and dephosphorized by the action of microorganisms in the tank in the biological reaction tank 1. Thus, organic substances, nitrogen components, and phosphorus components are reduced or removed.
次いで、生物反応槽１内の流入下水に相当する水量と、生物反応槽１に返送された汚泥量に相当する水量の処理液が、配管Ｌ４から最終沈殿池２に送られ、ここで沈降分離が行われる。最終沈殿池２では、ポリ塩化アルミニウム（ＰＡＣ）、塩化第二鉄（ＦｅＣｌ３）、硫酸バンド、ポリ硫酸第二鉄、重合珪酸―鉄塩（ＰＳＩ）、ポリアクリルアミド系高分子、カチオン系高分子、アルギン酸ナトリウム等の凝集剤を注入して、処理液を沈降分離させやすくしてもよい。 Next, a treatment liquid having an amount of water corresponding to the inflowing sewage in the biological reaction tank 1 and an amount of water corresponding to the amount of sludge returned to the biological reaction tank 1 is sent from the pipe L4 to the final settling basin 2, where sedimentation is performed. Is done. In the final sedimentation basin 2, polyaluminum chloride (PAC), ferric chloride (FeCl 3 ), sulfate band, polyferric sulfate, polymerized silicic acid-iron salt (PSI), polyacrylamide polymer, cationic polymer Alternatively, a flocculant such as sodium alginate may be injected to facilitate the precipitation of the treatment liquid.
そして、最終沈殿池２から汚泥の一部又は全部を配管Ｌ２から引き抜き、好ましくは、生物反応槽１への返送量が一定量となるように配管Ｌ２から引き抜いて返送し、その残部を配管Ｌ７から引き抜いて余剰汚泥として排出する。また、分離液は、配管Ｌ６から系外に放流する。 Then, a part or all of the sludge is pulled out from the final sedimentation basin 2 from the pipe L2, and is preferably pulled out from the pipe L2 and returned so that the return amount to the biological reaction tank 1 becomes a constant amount, and the remainder is piped L7. It is extracted from the waste water and discharged as excess sludge. Further, the separation liquid is discharged out of the system from the pipe L6.
一方、生物反応槽１への下水の流入水量が設計流入水量を超過する場合においては、以下のようにして処理が行われる。以下、設計流入水量をＱ、設計流水量を超過する水量をｑ、最終沈殿池２からの汚泥返送量をＳ１、活性汚泥濃縮装置３からの汚泥返送量をＳ２として説明する。 On the other hand, when the amount of sewage flowing into the biological reaction tank 1 exceeds the designed amount of flowing water, the treatment is performed as follows. Hereinafter, the design inflow water amount will be described as Q, the water amount exceeding the design flow water amount as q, the sludge return amount from the final sedimentation basin 2 as S1, and the sludge return amount from the activated sludge concentrator 3 as S2.
まず、生物反応槽１において、設計流入水量を超過する下水（水量：Ｑ＋ｑ）と最終沈殿池２からの汚泥返送量をＳ１、活性汚泥濃縮装置３からの汚泥返送量をＳ２が導入され、槽内の微生物の作用によって、脱窒処理、脱リン処理されて、有機物、窒素成分、リン成分が低減ないし除去される。 First, in the biological reaction tank 1, the sewage (water quantity: Q + q) exceeding the designed inflow water quantity and the sludge return quantity from the final sedimentation basin 2 are introduced into S1, and the sludge return quantity from the activated sludge concentrator 3 is introduced into S2. By the action of the microorganisms in the inside, denitrification treatment and dephosphorization treatment are performed, and organic substances, nitrogen components, and phosphorus components are reduced or removed.
次に、生物反応槽１からは、設計流入水量に相当する水量と、最終沈殿池２から生物反応槽１に返送された汚泥量に相当する水量の処理液（水量：Ｑ＋Ｓ１）が、配管Ｌ４から最終沈殿池２に供給され、設計流入水量を超過した水量と、活性汚泥濃縮装置３から生物反応槽１に返送された汚泥量に相当する水量の処理液（水量：ｑ＋Ｓ２）が、配管Ｌ５から引き抜かれて、活性汚泥濃縮装置３に供給される。 Next, from the biological reaction tank 1, a treatment liquid (water quantity: Q + S1) having an amount of water corresponding to the designed inflow water quantity and an amount of water equivalent to the amount of sludge returned from the final sedimentation tank 2 to the biological reaction tank 1 is supplied to the pipe L4. From the activated sludge concentrator 3 and the amount of water corresponding to the amount of sludge returned to the biological reactor 1 (water amount: q + S2) is supplied to the pipe L5. It is pulled out from and is supplied to the activated sludge concentrating device 3.
最終沈殿池２では、供給された処理液（水量：Ｑ＋Ｓ１）を、分離液と汚泥とに沈降分離させる。そして、最終沈殿池２から汚泥の一部又は全部を配管Ｌ２から引き抜き、好ましくは、生物反応槽１の汚泥濃度が低下しないように配管Ｌ２から引き抜いて生物反応槽１に返送し、その残部を配管Ｌ７から引き抜いて余剰汚泥として排出する。また、分離液は、配管Ｌ６から系外に放流する。 In the final sedimentation basin 2, the supplied treatment liquid (water amount: Q + S1) is settled and separated into a separation liquid and sludge. Then, part or all of the sludge is extracted from the final sedimentation basin 2 from the pipe L2, and is preferably extracted from the pipe L2 and returned to the biological reaction tank 1 so that the sludge concentration in the biological reaction tank 1 does not decrease. It is pulled out from the pipe L7 and discharged as excess sludge. Further, the separation liquid is discharged out of the system from the pipe L6.
活性汚泥濃縮装置３では、供給された処理液（水量：ｑ＋Ｓ２）を、分離液と活性汚泥濃縮液とに濃縮分離させる。そして、生物反応槽１から汚泥の全部を配管Ｌ３から引き抜き、好ましくは、生物反応槽１の汚泥濃度が低下しないように配管Ｌ３から引き抜いて生物反応槽１に返送する。また、分離液は、配管Ｌ８から系外に放流する。 In the activated sludge concentrating device 3, the supplied treatment liquid (water amount: q + S2) is concentrated and separated into a separated liquid and an activated sludge concentrated liquid. Then, the entire sludge is extracted from the biological reaction tank 1 from the pipe L3, and preferably is extracted from the pipe L3 and returned to the biological reaction tank 1 so that the sludge concentration in the biological reaction tank 1 does not decrease. Further, the separation liquid is discharged out of the system from the pipe L8.
この実施形態によれば、下水を生物反応槽１に供して生物反応処理すると共に、設計流入水量を超過した水量の処理液を活性汚泥濃縮装置３に送って分離液と活性汚泥濃縮液とに濃縮分離して活性汚泥濃縮液を生物反応槽に返送するようにしているので、生物反応槽１への下水の流入水量が設計流水量を超過した場合であっても、生物反応槽１内の活性汚泥濃度が低下しにくく、ほぼ一定濃度を維持できるので、生物反応槽１における下水の処理効率が損なわれにくい。また、最終沈殿池２には、設計量を超えた処理液は導入されないので、最終沈殿池２から排出される分離液には汚泥が流出しにくく、放流先の河川や海などへの影響が小さい。 According to this embodiment, the sewage is supplied to the biological reaction tank 1 for biological reaction treatment, and the treatment liquid having an amount of water exceeding the design inflow water amount is sent to the activated sludge concentrating device 3 to separate the separated liquid and the activated sludge concentrated liquid. Since the activated sludge concentrate is concentrated and separated and returned to the biological reaction tank, even if the amount of sewage flowing into the biological reaction tank 1 exceeds the designed flow volume, Since the activated sludge concentration is unlikely to decrease and can be maintained at a substantially constant concentration, the treatment efficiency of sewage in the biological reaction tank 1 is unlikely to be impaired. In addition, since the processing liquid exceeding the design amount is not introduced into the final sedimentation basin 2, sludge is unlikely to flow out into the separation liquid discharged from the final sedimentation basin 2, which has an influence on the discharge destination river or sea. small.
図２に、本発明の下水処理装置の第２の実施形態の概略構成図を示す。なお、上記第１の実施形態と実質的に同一部分には、同符号を付してその説明を省略することとする。 In FIG. 2, the schematic block diagram of 2nd Embodiment of the sewage treatment apparatus of this invention is shown. Note that substantially the same parts as those in the first embodiment are denoted by the same reference numerals, and description thereof is omitted.
この実施形態においては、活性汚泥濃縮装置３が、最終沈殿池２から伸びた配管Ｌ１０と接続している点が、上記第１の実施形態との相違点である。 In this embodiment, the point that the activated sludge concentrating device 3 is connected to the pipe L10 extending from the final settling basin 2 is a difference from the first embodiment.
生物反応槽１への下水の流入水量が設計流入水量以下の場合においては、上記第１の実施形態と同様に、配管Ｌ１から流入された下水が、生物反応槽１にて槽内の微生物の作用によって処理され、生物反応槽１内の流入下水に相当する水量と、最終沈殿池２から生物反応槽１に返送された汚泥量に相当する水量の処理液が、配管Ｌ４から最終沈殿池２に引き抜かれ、ここで沈降分離が行われる。そして、最終沈殿池２から汚泥の一部又は全部を配管Ｌ２から引き抜き、好ましくは、生物反応槽１の汚泥濃度が低下しないように配管Ｌ２から引き抜いて生物反応槽１に返送し、その残部を配管Ｌ７から引き抜いて余剰汚泥として排出させる。また、分離液は、配管Ｌ６から系外に放流される。 When the amount of sewage flowing into the biological reaction tank 1 is less than or equal to the designed inflow amount, the sewage that has flowed from the pipe L1 is transferred to the microorganisms in the tank in the biological reaction tank 1 as in the first embodiment. A treatment liquid having an amount of water corresponding to the inflowing sewage in the biological reaction tank 1 and an amount of water corresponding to the amount of sludge returned to the biological reaction tank 1 from the final sedimentation tank 2 from the pipe L4 is treated by the action. And the sedimentation separation takes place here. Then, part or all of the sludge is extracted from the final sedimentation basin 2 from the pipe L2, and is preferably extracted from the pipe L2 and returned to the biological reaction tank 1 so that the sludge concentration in the biological reaction tank 1 does not decrease. It is pulled out from the pipe L7 and discharged as excess sludge. Further, the separation liquid is discharged out of the system from the pipe L6.
一方、生物反応槽１への下水の流入水量が設計流入水量を超過する場合においては、まず、生物反応槽１において、設計流入水量を超過する下水（水量：Ｑ＋ｑ）と最終沈殿池２からの汚泥返送量をＳ１、活性汚泥濃縮装置３からの汚泥返送量をＳ２が導入されて、槽内の微生物の作用によって、脱窒処理、脱リン処理されて、有機物、窒素成分、リン成分が低減ないし除去される。 On the other hand, when the amount of inflow of sewage into the biological reaction tank 1 exceeds the designed inflow quantity, first, in the biological reaction tank 1, sewage (water quantity: Q + q) exceeding the designed inflow quantity and the final settling tank 2 The sludge return amount is S1 and the sludge return amount from the activated sludge concentrator 3 is introduced, and the denitrification treatment and the dephosphorization treatment are performed by the action of microorganisms in the tank to reduce the organic matter, the nitrogen component, and the phosphorus component. Or removed.
次に、生物反応槽１からは、生物反応槽１内の流入下水に相当する水量と、最終沈殿池２から生物反応槽１に返送された汚泥量に相当する水量と、活性汚泥濃縮装置３から生物反応槽１に返送された汚泥量に相当する水量の処理液（水量：Ｑ＋ｑ＋Ｓ１＋Ｓ２）が、配管Ｌ４から最終沈殿池２に送られる。 Next, from the biological reaction tank 1, the amount of water corresponding to the inflow sewage in the biological reaction tank 1, the amount of water corresponding to the amount of sludge returned from the final sedimentation basin 2 to the biological reaction tank 1, and the activated sludge concentrating device 3 A processing liquid (water amount: Q + q + S1 + S2) corresponding to the amount of sludge returned to the biological reaction tank 1 from the pipe L4 is sent to the final sedimentation tank 2.
最終沈殿池２では、設計流入水量を超過した水量と、活性汚泥濃縮装置３から生物反応槽１に返送された汚泥量に相当する水量の処理液（水量：ｑ＋Ｓ２）を配管Ｌ１０から引き抜いて活性汚泥濃縮装置３に供給すると共に、その残部の処理液［設計流入水量に相当する水量と、最終沈殿池２から生物反応槽１に返送された汚泥量に相当する水量の処理液（水量：Ｑ＋Ｓ１）］を、分離液と汚泥とに沈降分離させる。そして、最終沈殿池２から汚泥の一部又は全部を配管Ｌ２から引き抜き、好ましくは、生物反応槽１の汚泥濃度が低下しないように配管Ｌ２から引き抜いて生物反応槽１に返送し、その残部を配管Ｌ７から引き抜いて余剰汚泥として排出する。また、分離液は、配管Ｌ６から系外に放流する。 In the final sedimentation basin 2, a treatment liquid (water amount: q + S2) having a water amount exceeding the designed inflow water amount and a water amount corresponding to the sludge amount returned from the activated sludge concentrator 3 to the biological reaction tank 1 is extracted from the pipe L10 and activated. While supplying to the sludge concentrating device 3, the remaining treatment liquid [the amount of water corresponding to the designed inflow water amount and the amount of water corresponding to the amount of sludge returned from the final sedimentation tank 2 to the biological reaction tank 1 (water amount: Q + S1 )] Is settled and separated into a separated liquid and sludge. Then, part or all of the sludge is extracted from the final sedimentation basin 2 from the pipe L2, and is preferably extracted from the pipe L2 and returned to the biological reaction tank 1 so that the sludge concentration in the biological reaction tank 1 does not decrease. It is pulled out from the pipe L7 and discharged as excess sludge. Further, the separation liquid is discharged out of the system from the pipe L6.
活性汚泥濃縮装置３では、供給された処理液（水量：ｑ＋Ｓ２）を、分離液と活性汚泥濃縮液とに濃縮分離させる。そして、生物反応槽１から汚泥の全部を配管Ｌ３から引き抜き、好ましくは、生物反応槽１の汚泥濃度が低下しないように配管Ｌ３から引き抜いて生物反応槽１に返送する。また、分離液は、配管Ｌ８から系外に放流する。 In the activated sludge concentrating device 3, the supplied treatment liquid (water amount: q + S2) is concentrated and separated into a separated liquid and an activated sludge concentrated liquid. Then, the entire sludge is extracted from the biological reaction tank 1 from the pipe L3, and preferably is extracted from the pipe L3 and returned to the biological reaction tank 1 so that the sludge concentration in the biological reaction tank 1 does not decrease. Further, the separation liquid is discharged out of the system from the pipe L8.
この実施形態によれば、下水を生物反応槽１に供して生物反応処理すると共に、流入下水に相当する水量の処理液、すなわち生物反応槽での超過水量分を含む処理液を一旦最終沈殿池２に導入し、その後、最終沈殿池２から、設計流入水量を超過した水量の処理液を取り出して活性汚泥濃縮装置３へ送って分離液と活性汚泥濃縮液とに濃縮分離して活性汚泥濃縮液を生物反応槽に返送するようにしているので、生物反応槽１への下水の流入水量が設計流水量を超過した場合であっても、生物反応槽１内の活性汚泥濃度が低下しにくく、ほぼ一定濃度を維持できるので、生物反応槽１における下水の処理効率が損なわれにくい。また、活性汚泥濃縮装置３へ供給される処理液は、最終沈殿池２に導入した際に、多少なりとも処理が行われているので、活性汚泥濃縮装置３での装置負荷を低減できる。 According to this embodiment, the sewage is supplied to the biological reaction tank 1 for biological reaction treatment, and a treatment liquid having an amount of water corresponding to the inflowing sewage, that is, a treatment liquid containing an excess amount of water in the biological reaction tank is once used as a final sedimentation basin. 2 and then, from the final sedimentation basin 2, a treatment liquid with an amount exceeding the design inflow water volume is taken out and sent to the activated sludge concentrator 3 to concentrate and separate into a separated liquid and an activated sludge concentrated liquid to concentrate the activated sludge. Since the liquid is returned to the biological reaction tank, even if the amount of sewage flowing into the biological reaction tank 1 exceeds the designed flow volume, the activated sludge concentration in the biological reaction tank 1 is unlikely to decrease. Since a substantially constant concentration can be maintained, the treatment efficiency of sewage in the biological reaction tank 1 is not easily impaired. Moreover, since the process liquid supplied to the activated sludge concentration apparatus 3 is processed to some extent when it is introduced into the final sedimentation basin 2, the apparatus load on the activated sludge concentration apparatus 3 can be reduced.
この実施形態では、生物反応槽１への下水の流入水量が設計流入水量を超過する場合において、下水の流入水量が、生物反応槽の汚泥濃度が薄まると想定できる水量で、かつ、供給水量が反応槽容積の２０％以上のとき、好ましくは設計流入水量の２倍以上の時は、最終沈殿池２に処理液を供給すると同時に、設計流入水量を超過した水量の処理液を配管Ｌ１０から引き抜いて活性汚泥濃縮装置３に供給することが好ましい。 In this embodiment, when the inflow amount of sewage into the biological reaction tank 1 exceeds the designed inflow amount, the inflow quantity of sewage is an amount of water that can be assumed that the sludge concentration in the bioreactor tank becomes thin, and the supply water amount is When the volume of the reaction tank is 20% or more, preferably when it is more than twice the design inflow water amount, the treatment liquid is supplied to the final settling basin 2 and at the same time, the treatment liquid with an amount of water exceeding the design inflow water amount is drawn out from the pipe L10. The activated sludge concentrating device 3 is preferably supplied.
また、下水の流入水量が、生物反応槽の汚泥濃度が薄まらないと想定できる水量で、かつ、供給水量が反応槽容積の２０％以上のとき、好ましくは設計流入水量の２倍未満の時は、最終沈殿池２に汚泥が蓄積していき、汚泥が系外に流出する前に設計流入水量を超過した水量の処理液を配管Ｌ１０から引き抜いて活性汚泥濃縮装置３に供給することが好ましい。 In addition, when the amount of inflow of sewage is the amount of water that can be assumed that the sludge concentration in the biological reaction tank does not diminish, and the amount of supplied water is 20% or more of the reaction tank volume, it is preferably less than twice the design inflow water amount. At times, sludge accumulates in the final sedimentation basin 2, and before the sludge flows out of the system, a treatment liquid having an amount exceeding the design inflow water amount is withdrawn from the pipe L10 and supplied to the activated sludge concentrator 3. preferable.
以下、実施例を用いて本発明を更に詳細に説明する。 Hereinafter, the present invention will be described in more detail with reference to examples.
なお、以下の実施例、比較例において、流入下水として、下水処理場の最初沈殿池での処理水を用いた。また、下水処理装置での設計流入水量Ｑを、１．０ｍ３／日として処理を行った。また、生物反応槽１として標準活性汚泥法による処理槽を用いた。また、最終沈殿池２の水面積負荷を２０ｍ／日とした。活性汚泥濃縮装置３として、中空糸膜モジュールを用いた。 In the following examples and comparative examples, treated water in the first sedimentation basin of the sewage treatment plant was used as inflow sewage. In addition, the design inflow water quantity Q in the sewage treatment apparatus was treated as 1.0 m 3 / day. In addition, a treatment tank by a standard activated sludge method was used as the biological reaction tank 1. Moreover, the water area load of the final sedimentation basin 2 was 20 m / day. A hollow fiber membrane module was used as the activated sludge concentrating device 3.
（実施例１）
図１に示す下水処理装置を用いて下水処理を行った。配管Ｌ１から供給される流入下水の水量を１．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への送液量を１．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は約２０００ｍｇ／Ｌであり、最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１０ｍｇ／Ｌであった。なお、最終沈殿池２から返送される返送汚泥濃度は約６０００ｍｇ／Ｌであった。
Example 1
Sewage treatment was performed using the sewage treatment apparatus shown in FIG. The amount of incoming sewage supplied from the pipe L1 is 1.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the amount of liquid fed from the biological reaction tank 1 to the final sedimentation basin 2 is When operated as 1.5Q, the activated sludge concentration in the biological reaction tank 1 was about 2000 mg / L, and the effluent sludge concentration of the separation liquid discharged from the pipe L6 of the final sedimentation basin 2 was 10 mg / L. The return sludge concentration returned from the final sedimentation basin 2 was about 6000 mg / L.
また、配管Ｌ１から供給される流入下水の水量を２．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、配管Ｌ３から供給される活性汚泥濃縮装置３からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への処理液の送液量を１．５Ｑ、生物反応槽１から活性汚泥濃縮装置３への処理液の送液量を１．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は約２０００ｍｇ／Ｌであり、このとき最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１２ｍｇ／Ｌで、設計流水量で運転した場合とほぼ同程度であった。なお、最終沈殿池２及び活性汚泥濃縮装置３から返送される返送汚泥濃度は約６０００ｍｇ／Ｌであった。 Further, the amount of influent sewage supplied from the pipe L1 is 2.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the activated sludge concentrator 3 supplied from the pipe L3 The return sludge flow rate is 0.5Q, the amount of treatment liquid sent from the biological reaction tank 1 to the final sedimentation tank 2 is 1.5Q, and the amount of treatment liquid sent from the biological reaction tank 1 to the activated sludge concentrator 3 is 1. When operated as 5Q, the activated sludge concentration in the biological reaction tank 1 is about 2000 mg / L. At this time, the effluent sludge concentration of the separated liquid discharged from the pipe L6 of the final sedimentation basin 2 is 12 mg / L. It was almost the same as when driving in quantity. In addition, the returned sludge density | concentration returned from the final sedimentation basin 2 and the activated sludge concentration apparatus 3 was about 6000 mg / L.
（実施例２）
図２に示す下水処理装置を用いて下水処理を行った。配管Ｌ１から供給される流入下水の水量を１．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への送液量を１．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は約２０００ｍｇ／Ｌ、最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１０ｍｇ／Ｌであった。なお、最終沈殿池２から返送される返送汚泥濃度は約６０００ｍｇ／Ｌであった。
(Example 2)
Sewage treatment was performed using the sewage treatment apparatus shown in FIG. The amount of incoming sewage supplied from the pipe L1 is 1.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the amount of liquid fed from the biological reaction tank 1 to the final sedimentation basin 2 is When operated as 1.5Q, the activated sludge concentration in the biological reaction tank 1 was about 2000 mg / L, and the outflow sludge concentration of the separated liquid discharged from the pipe L6 of the final sedimentation basin 2 was 10 mg / L. The return sludge concentration returned from the final sedimentation basin 2 was about 6000 mg / L.
また、配管Ｌ１から供給される流入下水の水量を２．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、配管Ｌ３から供給される活性汚泥濃縮装置３からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への処理液の送液量を３．０Ｑ、最終沈殿池２から活性汚泥濃縮装置３への処理液の送液量を１．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は約２０００ｍｇ／Ｌであり、このとき最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１５ｍｇ／Ｌで、設計流水量で運転した場合とほぼ同程度であった。なお、最終沈殿池２及び活性汚泥濃縮装置３から返送される返送汚泥濃度は約６０００ｍｇ／Ｌであった。また、生物反応槽１から最終沈殿池２に処理液を供給するのとほぼ同時に最終沈殿池２から活性汚泥濃縮装置３に処理液を送液した。 Further, the amount of influent sewage supplied from the pipe L1 is 2.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the activated sludge concentrator 3 supplied from the pipe L3 The return sludge flow rate is 0.5Q, the amount of treatment liquid sent from the biological reaction tank 1 to the final sedimentation tank 2 is 3.0Q, and the amount of treatment liquid sent from the final sedimentation tank 2 to the activated sludge concentrator 3 is 1 When operated as 5Q, the activated sludge concentration in the biological reaction tank 1 is about 2000 mg / L. At this time, the effluent sludge concentration of the separated liquid discharged from the pipe L6 of the final sedimentation tank 2 is 15 mg / L. It was almost the same as when driving in quantity. In addition, the returned sludge density | concentration returned from the final sedimentation basin 2 and the activated sludge concentration apparatus 3 was about 6000 mg / L. In addition, the treatment liquid was fed from the final sedimentation tank 2 to the activated sludge concentrator 3 almost simultaneously with the supply of the treatment liquid from the biological reaction tank 1 to the final sedimentation tank 2.
（比較例１）
図３に示す、活性汚泥濃縮装置３を備えていない従来の下水処理装置を用いて下水処理を行った。
配管Ｌ１から供給される流入下水の水量を１．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への送液量を１．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は、約２０００ｍｇ／Ｌ、最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１０ｍｇ／Ｌであった。なお、最終沈殿池２から返送される返送汚泥濃度は約６０００ｍｇ／Ｌであった。
配管Ｌ１から供給される流入下水の水量を２．０Ｑ、配管Ｌ２から供給される最終沈殿池２からの返送汚泥流量を０．５Ｑ、生物反応槽１から最終沈殿池２への送液量を２．５Ｑとして運転したところ、生物反応槽１の活性汚泥濃度は、入口付近では約１５００ｍｇ／Ｌまで低下した。また、最終沈殿池２の配管Ｌ６から排出される分離液の流出汚泥濃度は１００ｍｇ／Ｌ以上となり、汚泥の流出が確認できた。なお、最終沈殿池２から返送される返送汚泥濃度は約８０００ｍｇ／Ｌであった。
(Comparative Example 1)
Sewage treatment was performed using a conventional sewage treatment apparatus that does not include the activated sludge concentration apparatus 3 shown in FIG.
The amount of incoming sewage supplied from the pipe L1 is 1.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the amount of liquid fed from the biological reaction tank 1 to the final sedimentation basin 2 is When operated as 1.5Q, the activated sludge concentration in the biological reaction tank 1 was about 2000 mg / L, and the effluent sludge concentration of the separated liquid discharged from the pipe L6 of the final sedimentation basin 2 was 10 mg / L. The return sludge concentration returned from the final sedimentation basin 2 was about 6000 mg / L.
The amount of influent sewage supplied from the pipe L1 is 2.0Q, the return sludge flow rate from the final sedimentation basin 2 supplied from the pipe L2 is 0.5Q, and the amount of liquid fed from the biological reaction tank 1 to the final sedimentation basin 2 is When operated as 2.5Q, the activated sludge concentration in the biological reaction tank 1 decreased to about 1500 mg / L in the vicinity of the inlet. Moreover, the outflow sludge density | concentration of the separation liquid discharged | emitted from the piping L6 of the final sedimentation basin 2 became 100 mg / L or more, and the outflow of sludge has been confirmed. The return sludge concentration returned from the final sedimentation basin 2 was about 8000 mg / L.
１：生物反応槽
２：最終沈殿池
３：活性汚泥濃縮装置
Ｌ１〜Ｌ１０：配管
1: Biological reaction tank 2: Final sedimentation tank 3: Activated sludge concentrator L1-L10: Piping
Claims (4)
前記生物反応槽への下水の流入水量が設計流入水量以下の場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池で沈降分離し、
前記生物反応槽への下水の流入水量が設計流入水量を超える場合、流入下水の全量を前記生物反応槽で生物処理した後、設計流入水量の処理液を前記最終沈殿池で沈降分離すると共に、設計流入水量を超過した水量の処理液を、前記最終沈殿槽に導入する前に活性汚泥濃縮装置に供給して分離液と活性汚泥濃縮液とに濃縮分離し、この活性汚泥濃縮液を前記生物反応槽に返送することを特徴とする下水処理方法。 In a sewage treatment method in which sewage is biologically treated in a biological reaction tank, and the treatment liquid is settled and separated into a separation liquid and sludge in a final sedimentation basin,
If the amount of sewage inflow into the biological reaction tank is less than or equal to the design inflow water, the entire amount of inflow sewage is biologically treated in the biological reaction tank, and then the entire amount of the treated liquid is settled and separated in the final sedimentation basin,
When the amount of sewage inflow into the bioreactor exceeds the design inflow, the entire amount of inflow sewage is biologically treated in the bioreactor, and then the treatment liquid of the design inflow is settled and separated in the final sedimentation basin, Before introducing into the final sedimentation tank, a treatment liquid having an amount of water that exceeds the design inflow water volume is supplied to the activated sludge concentrator and concentrated and separated into a separated liquid and an activated sludge concentrated liquid. A sewage treatment method, which is returned to a reaction tank.
前記生物反応槽への下水の流入水量が設計流入水量以下の場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池で沈降分離し、
前記生物反応槽への下水の流入水量が設計流入水量を超える場合、流入下水の全量を前記生物反応槽で生物処理した後、その処理液の全量を最終沈殿池に供給し、その後前記最終沈殿池から設計流入水量を超過した水量の処理液を取り出して活性汚泥濃縮装置に供給して分離液と活性汚泥濃縮液とに濃縮分離し、この活性汚泥濃縮液を前記生物反応槽に返送すると共に、前記残った処理液を前記最終沈殿池で沈降分離することを特徴とする下水処理方法。 In a sewage treatment method in which sewage is biologically treated in a biological reaction tank, and the treatment liquid is settled and separated into a separation liquid and sludge in a final sedimentation basin,
If the amount of sewage inflow into the biological reaction tank is less than or equal to the design inflow water, the entire amount of inflow sewage is biologically treated in the biological reaction tank, and then the entire amount of the treated liquid is settled and separated in the final sedimentation basin,
When the amount of sewage inflow into the bioreactor exceeds the design inflow, the entire amount of inflow sewage is biologically treated in the bioreactor, and then the entire amount of the treated liquid is supplied to the final sedimentation basin, and then the final precipitation A processing liquid with an amount exceeding the design inflow water amount is taken out from the pond, supplied to the activated sludge concentrator, concentrated and separated into a separated liquid and an activated sludge concentrated liquid, and this activated sludge concentrated liquid is returned to the biological reaction tank. The sewage treatment method is characterized in that the remaining treatment liquid is settled and separated in the final sedimentation basin.
生物処理後の処理液を分離液と汚泥に沈降分離する最終沈殿池と、
生物処理後の処理液を分離液と活性汚泥濃縮液に濃縮分離する活性汚泥濃縮装置と、
前記生物反応槽から前記最終沈殿池に処理液を通水させる第１の通水経路と、
設計流入水量を超過した水量の処理液を、前記生物反応槽から活性汚泥濃縮装置に通水させる第２の通水経路と、
前記最終沈殿池から前記生物反応槽に前記汚泥を返送する第１の返送経路と、
前記活性汚泥濃縮装置から前記生物反応槽に前記活性汚泥濃縮液を返送する第２の返送経路とを備えることを特徴とする下水処理装置。 A biological reactor for biological treatment of sewage,
A final sedimentation basin that settles and separates the treatment liquid after biological treatment into a separation liquid and sludge;
An activated sludge concentrator that concentrates and separates the treatment liquid after biological treatment into a separated liquid and an activated sludge concentrate;
A first water flow path for passing a treatment liquid from the biological reaction tank to the final sedimentation basin;
A second water flow path for passing a treatment liquid having an amount exceeding the design inflow water amount from the biological reaction tank to the activated sludge concentrator;
A first return path for returning the sludge from the final sedimentation basin to the biological reaction tank;
A sewage treatment apparatus comprising: a second return path for returning the activated sludge concentrate from the activated sludge concentrator to the biological reaction tank.
生物処理後の処理液を分離液と汚泥に沈降分離する最終沈殿池と、
生物処理後の処理液を分離液と活性汚泥濃縮液に濃縮分離する活性汚泥濃縮装置と、
前記生物反応槽から前記最終沈殿池に処理液を通水させる第１の通水経路と、
設計流入水量を超過した水量の処理液を、前記最終沈殿池から活性汚泥濃縮装置に通水させる第２の通水経路と、
前記最終沈殿池から前記生物反応槽に前記汚泥を返送する第１の返送経路と、
前記活性汚泥濃縮装置から前記生物反応槽に前記活性汚泥濃縮液を返送する第２の返送経路とを備えることを特徴とする下水処理装置。 A biological reactor for biological treatment of sewage,
A final sedimentation basin that settles and separates the treatment liquid after biological treatment into a separation liquid and sludge;
An activated sludge concentrator that concentrates and separates the treatment liquid after biological treatment into a separated liquid and an activated sludge concentrate;
A first water flow path for passing a treatment liquid from the biological reaction tank to the final sedimentation basin;
A second water flow path for passing a treatment liquid having an amount exceeding the design inflow water amount from the final settling basin to the activated sludge concentrator;
A first return path for returning the sludge from the final sedimentation basin to the biological reaction tank;
A sewage treatment apparatus comprising: a second return path for returning the activated sludge concentrate from the activated sludge concentrator to the biological reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2007078058A JP5091515B2 (en) | 2007-03-26 | 2007-03-26 | Sewage treatment method and sewage treatment apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2007078058A JP5091515B2 (en) | 2007-03-26 | 2007-03-26 | Sewage treatment method and sewage treatment apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2008237958A true JP2008237958A (en) | 2008-10-09 |
| JP5091515B2 JP5091515B2 (en) | 2012-12-05 |
Family
ID=39909937
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2007078058A Expired - Fee Related JP5091515B2 (en) | 2007-03-26 | 2007-03-26 | Sewage treatment method and sewage treatment apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP5091515B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012245457A (en) * | 2011-05-26 | 2012-12-13 | Metawater Co Ltd | Sewage treatment method and sewage treatment apparatus |
| JP2013188650A (en) * | 2012-03-12 | 2013-09-26 | Toshiba Corp | Water treatment system and water treatment method |
| WO2014034827A1 (en) * | 2012-08-31 | 2014-03-06 | 東レ株式会社 | Fresh water generation method |
Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09206793A (en) * | 1996-02-05 | 1997-08-12 | Kubota Corp | Sewage treatment and sewage treating device |
| JPH09220595A (en) * | 1996-02-14 | 1997-08-26 | Kubota Corp | Sewage treatment method and apparatus |
| JP2000140878A (en) * | 1998-11-05 | 2000-05-23 | Nishihara Environ Sanit Res Corp | Waste water treating device |
| JP2000301198A (en) * | 1999-04-15 | 2000-10-31 | Mitsubishi Kakoki Kaisha Ltd | Volume reducing treatment of sludge |
| JP2001219193A (en) * | 2000-02-09 | 2001-08-14 | Ngk Insulators Ltd | Method and apparatus for treating sewage in confluent type sewerage |
| JP2003088885A (en) * | 2001-09-18 | 2003-03-25 | Ebara Corp | Method and apparatus for treating organic waste water |
| JP2003136088A (en) * | 2001-11-06 | 2003-05-13 | Ngk Insulators Ltd | Sewage treatment method and apparatus in confluent type sewerage |
| JP2003154211A (en) * | 2001-11-21 | 2003-05-27 | Ngk Insulators Ltd | Method of treating uncertain water in separated sewer system |
| JP2004041953A (en) * | 2002-07-12 | 2004-02-12 | Mitsubishi Kakoki Kaisha Ltd | Method and equipment for treating organic waste water |
| JP2004255268A (en) * | 2003-02-25 | 2004-09-16 | Kurita Water Ind Ltd | Waste water treatment apparatus |
| JP2005021725A (en) * | 2003-06-30 | 2005-01-27 | Tsukishima Kikai Co Ltd | Sewage treatment equipment and sewage treatment method |
| JP2005034763A (en) * | 2003-07-16 | 2005-02-10 | Ngk Insulators Ltd | Reconstruction method of existing sewage treatment plant |
| JP2005218991A (en) * | 2004-02-06 | 2005-08-18 | Unitika Ltd | Filtration treatment method in combined sewer system |
| JP2007038092A (en) * | 2005-08-02 | 2007-02-15 | Ngk Insulators Ltd | Apparatus and method for treatment of sewage in rainy weather and secondary effluent |
| JP2007050375A (en) * | 2005-08-19 | 2007-03-01 | Mitsubishi Rayon Eng Co Ltd | Wastewater treatment apparatus and wastewater treatment method |
| JP2008000697A (en) * | 2006-06-23 | 2008-01-10 | Ngk Insulators Ltd | Primary treatment method of combined sewage |
-
2007
- 2007-03-26 JP JP2007078058A patent/JP5091515B2/en not_active Expired - Fee Related
Patent Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09206793A (en) * | 1996-02-05 | 1997-08-12 | Kubota Corp | Sewage treatment and sewage treating device |
| JPH09220595A (en) * | 1996-02-14 | 1997-08-26 | Kubota Corp | Sewage treatment method and apparatus |
| JP2000140878A (en) * | 1998-11-05 | 2000-05-23 | Nishihara Environ Sanit Res Corp | Waste water treating device |
| JP2000301198A (en) * | 1999-04-15 | 2000-10-31 | Mitsubishi Kakoki Kaisha Ltd | Volume reducing treatment of sludge |
| JP2001219193A (en) * | 2000-02-09 | 2001-08-14 | Ngk Insulators Ltd | Method and apparatus for treating sewage in confluent type sewerage |
| JP2003088885A (en) * | 2001-09-18 | 2003-03-25 | Ebara Corp | Method and apparatus for treating organic waste water |
| JP2003136088A (en) * | 2001-11-06 | 2003-05-13 | Ngk Insulators Ltd | Sewage treatment method and apparatus in confluent type sewerage |
| JP2003154211A (en) * | 2001-11-21 | 2003-05-27 | Ngk Insulators Ltd | Method of treating uncertain water in separated sewer system |
| JP2004041953A (en) * | 2002-07-12 | 2004-02-12 | Mitsubishi Kakoki Kaisha Ltd | Method and equipment for treating organic waste water |
| JP2004255268A (en) * | 2003-02-25 | 2004-09-16 | Kurita Water Ind Ltd | Waste water treatment apparatus |
| JP2005021725A (en) * | 2003-06-30 | 2005-01-27 | Tsukishima Kikai Co Ltd | Sewage treatment equipment and sewage treatment method |
| JP2005034763A (en) * | 2003-07-16 | 2005-02-10 | Ngk Insulators Ltd | Reconstruction method of existing sewage treatment plant |
| JP2005218991A (en) * | 2004-02-06 | 2005-08-18 | Unitika Ltd | Filtration treatment method in combined sewer system |
| JP2007038092A (en) * | 2005-08-02 | 2007-02-15 | Ngk Insulators Ltd | Apparatus and method for treatment of sewage in rainy weather and secondary effluent |
| JP2007050375A (en) * | 2005-08-19 | 2007-03-01 | Mitsubishi Rayon Eng Co Ltd | Wastewater treatment apparatus and wastewater treatment method |
| JP2008000697A (en) * | 2006-06-23 | 2008-01-10 | Ngk Insulators Ltd | Primary treatment method of combined sewage |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012245457A (en) * | 2011-05-26 | 2012-12-13 | Metawater Co Ltd | Sewage treatment method and sewage treatment apparatus |
| JP2013188650A (en) * | 2012-03-12 | 2013-09-26 | Toshiba Corp | Water treatment system and water treatment method |
| WO2014034827A1 (en) * | 2012-08-31 | 2014-03-06 | 東レ株式会社 | Fresh water generation method |
| JPWO2014034827A1 (en) * | 2012-08-31 | 2016-08-08 | 東レ株式会社 | Fresh water generation method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP5091515B2 (en) | 2012-12-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7713417B2 (en) | Method for wastewater treatment with resource recovery and reduced residual solids generation | |
| KR101804555B1 (en) | WasteWater High-Class Treatment System to remove High-Density Pollutant and Method thereof | |
| US7563373B2 (en) | Removal of phosphorous from wastewater | |
| US20070003370A1 (en) | A method for treating landfill leachate | |
| WO2007077776A1 (en) | Apparatus and method for treating organic-containing wastewater | |
| KR101373881B1 (en) | Apparatus and method for treatment of organic substance-containing wastewater | |
| US8105490B2 (en) | Low phosphorus water treatment systems | |
| WO2012042524A1 (en) | Treatment for molasses spent wash and other wastewaters | |
| KR101463987B1 (en) | Method of treating organic waste water | |
| CN109293145A (en) | The method that textile waste is back to Thermal Power Generation Industry | |
| JP5091515B2 (en) | Sewage treatment method and sewage treatment apparatus | |
| JP2007196137A (en) | Treatment method and apparatus for biologically treated water | |
| JP2007050387A (en) | Apparatus for treating organic waste liquor | |
| KR100817041B1 (en) | Wastewater processing apparatus employing a deposition device and a biological filtering device | |
| KR0168827B1 (en) | Method for purifying organic waste water | |
| JP2008307494A (en) | Sewage treating method and sewage treatment apparatus | |
| US11661366B2 (en) | Process for selenium removal with biological, chemical and membrane treatment | |
| KR100911443B1 (en) | System for treatment of wastewater and method for treatment of wastewater using the same | |
| JP5876671B2 (en) | Sewage treatment method and sewage treatment apparatus | |
| JP2002316191A (en) | Method and apparatus for treating organic foul water | |
| KR20200087397A (en) | Treatment system of waste water using oxidation preprocess | |
| JP2007260515A (en) | Sludge separator and sludge separation method | |
| CN218810945U (en) | Aged stock landfill leachate treatment system | |
| CA2555875C (en) | Removal of phosphorous from wastewater | |
| JP7195968B2 (en) | Method for operating organic wastewater treatment equipment and organic wastewater treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20091204 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20101122 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20120904 |
|
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20120914 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20150921 Year of fee payment: 3 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 5091515 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20150921 Year of fee payment: 3 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| LAPS | Cancellation because of no payment of annual fees |