JPS63302996A - Treatment of organic sewage - Google Patents
Treatment of organic sewageInfo
- Publication number
- JPS63302996A JPS63302996A JP62138986A JP13898687A JPS63302996A JP S63302996 A JPS63302996 A JP S63302996A JP 62138986 A JP62138986 A JP 62138986A JP 13898687 A JP13898687 A JP 13898687A JP S63302996 A JPS63302996 A JP S63302996A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- water
- denitrification
- bod
- slurry
- 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 1
- 238000000034 method Methods 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000012528 membrane Substances 0.000 claims abstract description 31
- 239000002002 slurry Substances 0.000 claims abstract description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 9
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims abstract description 5
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052698 phosphorus Inorganic materials 0.000 claims description 10
- 239000011574 phosphorus Substances 0.000 claims description 10
- 239000002351 wastewater Substances 0.000 claims description 5
- 230000000813 microbial effect Effects 0.000 claims description 3
- 239000010802 sludge Substances 0.000 abstract description 29
- 239000011575 calcium Substances 0.000 abstract description 6
- 238000010276 construction Methods 0.000 abstract description 2
- 239000002689 soil Substances 0.000 abstract 2
- 239000010800 human waste Substances 0.000 description 15
- 230000000694 effects Effects 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical class [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 5
- 239000001506 calcium phosphate Substances 0.000 description 4
- 229910000389 calcium phosphate Inorganic materials 0.000 description 4
- 235000011010 calcium phosphates Nutrition 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 210000002700 urine Anatomy 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 206010011224 Cough Diseases 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- HLCFGWHYROZGBI-JJKGCWMISA-M Potassium gluconate Chemical compound [K+].OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C([O-])=O HLCFGWHYROZGBI-JJKGCWMISA-M 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052588 hydroxylapatite Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- XYJRXVWERLGGKC-UHFFFAOYSA-D pentacalcium;hydroxide;triphosphate Chemical compound [OH-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O XYJRXVWERLGGKC-UHFFFAOYSA-D 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 150000003016 phosphoric acids Chemical class 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Removal Of Specific Substances (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、し尿系汚水その他のリンと窒素成分を含む有
機性汚水を新規なプロセスにより合理的に処理し、常に
安定して高度の処理水を得る方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention is designed to rationally treat human waste water and other organic wastewater containing phosphorus and nitrogen components using a new process, and to always achieve stable and high-level treatment. It concerns how to obtain water.
〔従来技術および発明が解決しようとする問題点〕し尿
系汚水等を処理するのに、最も代表的なプロセスは、
というプロセスであるが、このプロセスは固液分離が不
安定で、かつ難脱水性の凝集沈殿汚泥が大量に発生する
という大きな欠点があった。[Prior art and problems to be solved by the invention] The most typical process for treating human waste water, etc. is the following process, but this process has unstable solid-liquid separation and is difficult to dewater. The major drawback was that a large amount of coagulated and precipitated sludge was generated.
一方、ごく最近では、
という新しいプロセスが提案され、数ケ所で実用化され
た。このプロセスは、固液分離が確実てあり、しかも凝
集沈殿工程が不要であるという長所がある反面、ｐｌ＋
調整、再中和、吸着材の再生及び再生廃液の処分という
繁雑な工程を必要とするリン吸着除去工作を限外濾過（
ＵＦ）膜分離工程のあとに配備しなければならないとい
う欠点をもっている。On the other hand, very recently, a new process has been proposed and put into practical use in several places. This process has the advantage of ensuring solid-liquid separation and does not require a coagulation-sedimentation step.
Ultrafiltration (
UF) has the disadvantage that it must be installed after the membrane separation process.
このようなリン吸着除去工程を設けなくてはならない理
由は、ＵＦ膜ではＰ０４′−が全く除去されずにそのま
ま透過してしまうためであり、これがＵＰ膜を使う活性
汚泥処理法の最大の問題点であった。The reason why such a phosphorus adsorption/removal process is necessary is that P04'- is not removed at all in the UF membrane and passes through as it is, and this is the biggest problem with the activated sludge treatment method using the UP membrane. It was a point.
本発明は、これらの従来法のもつ問題点を解決すること
をｉ！！題としており、具体的には、■ 凝集沈殿処理
を省略してなおかつ充分なリン除去率を得ること。The present invention aims to solve the problems of these conventional methods. ! Specifically, (1) Omit the coagulation-sedimentation treatment and still obtain a sufficient phosphorus removal rate.
■ ＵＦ膜分離工程のあとに、ＰＯｅ−吸着除去上。■ After the UF membrane separation process, on POe-adsorption removal.
程を設けることを不要にすること。To make it unnecessary to set a time limit.
■ 汚泥の脱水性を改善すること。■ Improving the dewatering properties of sludge.
■ プロセス構成を一層簡潔化すること。■ Further simplify the process configuration.
■ 汚泥の肥料的価値を高めること。すなわち、植物に
とって利用容易な形態のリン酸化合物を豊富に含んだ汚
泥脱水ケーキを生産すること。■ Increasing the fertilizer value of sludge. That is, to produce a sludge dewatering cake rich in phosphoric acid compounds in a form that is easily usable by plants.
■ 水酸化アルミ、水酸化鉄などのバルキーで難濃縮脱
水性汚泥の発生を防ぎ、汚泥処理工程を合理化すること
。■ Preventing the generation of bulky, difficult-to-thicken and dewaterable sludge such as aluminum hydroxide and iron hydroxide, and streamlining the sludge treatment process.
を解決課題としている。is the problem to be solved.
本発明は、リン及び窒素成分を含む有機性ｌη水を生物
学的硝化脱窒素工程で処理する方法において、ＢＯ［）
、窒素成分の少なくとも大部分を除去し、カルシウム
イオンの共存下で咳微生吻スラリを水？ｎ３０〜４５℃
、ｐＨ７，５〜９．５の条件下に維持したのち膜分離し
、分離された膜分離スラリを前記生物学的硝化脱窒素工
程に返送することを特徴とする有機性汚水の処理方法で
ある。The present invention provides a method for treating organic lη water containing phosphorus and nitrogen components in a biological nitrification and denitrification process, in which BO[)
, remove at least most of the nitrogen components and water the cough micronasal slurry in the coexistence of calcium ions? n30~45℃
, a method for treating organic wastewater characterized by maintaining it under conditions of pH 7.5 to 9.5, performing membrane separation, and returning the separated membrane-separated slurry to the biological nitrification and denitrification process. .
以下に本発明の一実施態様を示す図面を参照しながら、
し尿処理を例にあげて本発明の作用を詳述する。With reference to the drawings showing one embodiment of the invention below,
The effect of the present invention will be explained in detail by taking human waste treatment as an example.
まず、し尿１をスクリーン２によって除清し、除渣し尿
３を得る。この除渣し尿３を希釈することなく、硝化ｅ
、循環型の生物学的１ｉ１’ｌ化脱窒素工程４に供給し
て生物学的脱窒素処理し、除渣し尿３中のＢＯＤ、窒素
成分の大部分は該工程４の第１脱窒素槽５と硝化槽６に
おいて除去される。次に硝化槽６から流出する活性汚泥
スラリを第２脱窒素槽７に導いてカルシウムイオン（Ｃ
ａ” ）が不足している時はＣａ”Ｒ８（ＣａＣ１１Ｃ
ａ５Ｏａ、 Ｃａ（ＯＨ）ｔ。First, human waste 1 is removed using a screen 2 to obtain removed human waste 3. Nitrification e
, is supplied to a circulating biological denitrification process 4 for biological denitrification treatment, and most of the BOD and nitrogen components in the removed human urine 3 are transferred to the first denitrification tank of the process 4. 5 and nitrification tank 6. Next, the activated sludge slurry flowing out from the nitrification tank 6 is guided to the second denitrification tank 7, and calcium ions (C
a”) is insufficient, Ca”R8 (CaC11C
a5Oa, Ca(OH)t.
ＣａＯなどから選択する）を添加し、この第２脱窒素槽
７における水温を３０〜４５℃、ｐｌ＋を７．５〜９．
５にコントロールし、所定時間（２日間程度に設定する
のがよい）活性汚泥スラリを滞留させ、その後再曝気槽
９において少量の残留ＢＯＤ、 Ｎｌ１３−Ｎを酸化す
る。(selected from CaO, etc.), and the water temperature in the second denitrification tank 7 was set at 30-45°C, and the pl+ was set at 7.5-9.
5, the activated sludge slurry is allowed to stagnate for a predetermined period of time (preferably about 2 days), and then a small amount of residual BOD and Nl13-N are oxidized in the re-aeration tank 9.
なお、Ｃａ２１源８は第２脱窒素槽７へでなく、再曝気
槽９に添加しても、あるいは第２脱窒素槽７と再曝気槽
９の両槽に添加してもよく、後述する膜分離工程ｌＯの
前ならいかなる点においてもよい。また硝化槽６から流
出する活性汚泥スラリ中に残留するＢＯＤ 、 ＮＨ，
−Ｎが無視少のときは再曝気槽９を省略することができ
る。Note that the Ca21 source 8 may be added to the reaeration tank 9 instead of the second denitrification tank 7, or may be added to both the second denitrification tank 7 and the reaeration tank 9, which will be described later. Any point before the membrane separation step IO may be used. In addition, BOD, NH, remaining in the activated sludge slurry flowing out from the nitrification tank 6
- When N is negligible, the reaeration tank 9 can be omitted.
このような水温、ｐＨの特定範囲において、Ｃａ １
＋の共存下で活性汚泥スラリを所要時間（５〜４８時間
が効果的である）滞留せしめると、し尿中のＰＯ４１は
ハイドロキシアパタイトなどのリン酸カルシウム系化合
物ＳＳに変化し、このＳＳは後続して設けられたＯＦ膜
、精密１月過側Ｆ）膜などの膜分離工程ｌＯによって、
活性汚泥スラリとともに完全に分離捕捉され、ＳＳゼロ
の膜ｉ！ｉ過水１１が得られる。In such a specific range of water temperature and pH, Ca 1
When the activated sludge slurry is allowed to stay for the required time (effectively 5 to 48 hours) in the presence of +, PO41 in human waste changes to calcium phosphate compounds SS such as hydroxyapatite, and this SS is subsequently added. Through the membrane separation process lO, such as filtrated OF membranes and precision membranes,
Membrane i! completely separates and captures the activated sludge slurry and has zero SS! i Perhydrogen 11 is obtained.
この膜分離工程１０で得られた膜透過水１１は、し尿中
の８００ 、 ＣＯＤ 、窒素成分、ＳＳ及びｐｏ、’
−などが高度に除去されており、そのまま放流可能な水
質を示すが、難生物分解性のＣＯＤ成分が１００ｏｖ／
ｅ程度残留することがあるので、所望に応じて活性炭吸
着処理を行ったのち放流してもよい。The membrane permeated water 11 obtained in this membrane separation step 10 contains 800, COD, nitrogen components, SS and po,' in human waste.
- etc. have been removed to a high degree, indicating a water quality that can be discharged as is, but the COD component, which is difficult to biodegrade,
Since about 50% of the water may remain, if desired, it may be treated with activated carbon adsorption before being discharged.
一方、膜分離工程１０で分離された膜分離スラリ１２の
大部分は返送汚泥１３として生物学的硝化脱窒素工程４
の第１脱窒素槽５に返送され、余った余剰汚泥１４は汚
泥脱水工程１５（ベルトプレス、遠心脱水機、フィルタ
プレス、スクリュープレスなどを採用する）に供給され
、脱水ケーキ１６と脱水分離水１７に分離され、脱水分
離水１７は再曝気槽９又は第２脱窒素槽７にリサイクル
される。On the other hand, most of the membrane separation slurry 12 separated in the membrane separation step 10 is returned to the biological nitrification and denitrification step 13 as return sludge 13.
The surplus sludge 14 is returned to the first denitrification tank 5, and the remaining surplus sludge 14 is supplied to the sludge dewatering process 15 (adopting a belt press, centrifugal dehydrator, filter press, screw press, etc.), where it is dehydrated cake 16 and dehydrated separated water. The dehydrated separated water 17 is recycled to the reaeration tank 9 or the second denitrification tank 7.
また上記実施態様においては、生物学的硝化脱窒素工程
４に硝化液循環方式を採用しであるが、必ずしも硝化液
循環方式に限らず他の公知の方式を採用することができ
る。その場合の方式によっては、ＢＯＤ 、 ＮＨ３−
Ｎの除去処理をすべて完了して流出する微生物スラリ中
にＣａ”°を添加し、このスラリを別途滞留槽で前記水
温、ｐｌ＋条件下に維持するもよい。Further, in the embodiment described above, a nitrification solution circulation method is adopted in the biological nitrification and denitrification step 4, but the method is not necessarily limited to the nitrification solution circulation method, and other known methods can be adopted. Depending on the method in that case, BOD, NH3-
It is also possible to add Ca''° to the microbial slurry that flows out after completing the N removal process, and maintain this slurry at the water temperature and pl+ conditions in a separate retention tank.
本発明において、Ｃａ”が添加された微生物スラリを前
述した特定水温及びｐｌ＋条件下に維持することは非常
に重要であり、水温が３０℃未満であると、ＰＯａ３−
除去率が悪化し、水温が４５℃を超えるとその後返送さ
れる■々膜分離スラリ１２中微生物の硝化活性が悪化す
る。また、ｐＨが７．５未満ではやはりＰＯ４３−除去
率が悪化し、ｐＨが９．５を超えると膜分離スラリ１２
中の微生物の硝化、脱窒素活性が悪化する。In the present invention, it is very important to maintain the microbial slurry to which Ca'' has been added under the above-mentioned specific water temperature and pl+ conditions; if the water temperature is less than 30℃, POa3-
When the removal rate deteriorates and the water temperature exceeds 45° C., the nitrification activity of microorganisms in the membrane-separated slurry 12 that is subsequently returned deteriorates. In addition, if the pH is less than 7.5, the PO43 removal rate will deteriorate, and if the pH exceeds 9.5, the membrane separation slurry 12
The nitrification and denitrification activities of the microorganisms inside deteriorate.
さらに本発明において発生する余剰汚泥１４は、Ａ １
（Ｏｉｌ） ｙ、Ａ Ｉ ＰＯａなどのような極めて
ｉｉ１濃縮脱水性の無機汚泥を全く含んでおらず、逆に
脱水性のよいリン酸カルシウム系のスラッジを共存して
いるので、余剰汚泥１３の脱水性は良好であり、脱水ケ
ーキ水分はアルミニウム系無機汚泥などを含有する汚泥
よりも数％低下する。しかも脱水ケーキ１６には、リン
が植物によって容易に利用できるリン酸カルシウムの形
態で豊富に含有されていることも本発明の重要な特長で
ある（Ａ Ｉ ＰＯａの形態のリンは植物によって吸収
されない）。Furthermore, the surplus sludge 14 generated in the present invention is A 1
(Oil) It does not contain any highly concentrated dewaterable inorganic sludge such as y, A I POa, etc., and on the contrary, it coexists with calcium phosphate sludge that has good dewatering properties, so the dewaterability of surplus sludge 13 is The moisture content of the dehydrated cake is several percent lower than that of sludge containing aluminum-based inorganic sludge. Moreover, it is an important feature of the present invention that the dehydrated cake 16 contains abundant phosphorus in the form of calcium phosphate, which can be easily utilized by plants (phosphorus in the form of A I POa is not absorbed by plants).
神奈川系Ｚ市し尿処理場に搬入されたし尿を目開き０．
５鶴目のロータリウェッジワイヤスクリーンで除渣し、
表−１の水質を示す除渣し尿を得た。Human waste transported to the Z city human waste treatment plant in the Kanagawa region is collected with a mesh size of 0.
Remove the residue with a rotary wedge wire screen with a fifth crane.
Removal of human urine with water quality shown in Table 1 was obtained.
表−１除渣し尿水質
この除渣し尿を、硝化液循環タイプの生物学的硝化脱窒
素工程（第１脱窒素槽−硝化槽一第２脱窒素槽−再曝気
槽の順に直列配置したもの）に供給し、活性汚泥ＭＬＳ
Ｓ １２０００■／１、し尿温留日数１０日間、硝化液
循環量２６〜３０Ｑｍ／日（Ｑはし尿処理量２７日）、
水！３０°〜４５℃の条件で無希釈生物処理を行なった
０次にこの活性汚泥スラリを滞留時間２日の第２脱窒素
槽でＣａＣ１ｚを８００ ＝１５００■／ ｊ！ａｓＣ
ａ”添加し、さらにＮａ０ｌｌでｐＨを８．０〜８．５
に制御した０次いでこの活性汚泥スラリを滞留時間１日
の再曝気槽を経由せしめたのちチューブラ型ＵＦ膜（分
画分子量約４００００）にポンプ圧入し、スラリをクロ
スフローフィルトレージョンで膜分離した。この時のＵ
Ｆ膜透過水量は１．２イ／ｍ′膜面積・日が得られ、Ｕ
Ｐ膜透過水の水質は表−２のように極めて良好であった
。Table 1: Water quality of removed human waste This removed human waste is used in a biological nitrification and denitrification process using a nitrification liquid circulation type (1st denitrification tank - nitrification tank - 2nd denitrification tank - 2nd denitrification tank - reaeration tank arranged in series) ) and activated sludge MLS
S 12000■/1, human waste retention period 10 days, nitrified fluid circulation amount 26-30 Qm/day (Q human waste processing amount 27 days),
water! This activated sludge slurry, which was subjected to undiluted biological treatment under the conditions of 30° to 45°C, was stored in a second denitrification tank with a residence time of 2 days to reduce CaC1z to 800 = 1500■/j! asC
a” and further adjust the pH to 8.0 to 8.5 with Na0ll.
The activated sludge slurry was passed through a re-aeration tank with a residence time of 1 day, then pumped into a tubular UF membrane (molecular weight cut off: approximately 40,000), and the slurry was membrane-separated by cross-flow filtration. . U at this time
The amount of water permeated through the F membrane is 1.2 i/m' membrane area/day, and U
The quality of the water permeated through the P membrane was extremely good as shown in Table 2.
表−２膜透過水水質
また、ＵＦ膜にて分離された膜分離スラリを生物学的硝
化脱窒素工程の第１脱窒素槽に返送し、その余剰分Ｃ５
５ｆＨ度約２％）にＤＡＭ系（ポリ・ジアルキルアミノ
・エチルメタクリレート系）のカオオンボリマーを１．
０％ｔｏ ＳＳ 添加してフロック形成したのち、ロ
ールプレス型脱水機〔荏原インフィルコ■製品デバイロ
ール〕で脱水したところリン酸カルシウムを含む水分７
２〜７４％の低水分の脱水ケーキが得られ、脱水分離水
は再曝気槽にリサイクルさせた。Table 2 Membrane permeate water quality In addition, the membrane separated slurry separated by the UF membrane is returned to the first denitrification tank of the biological nitrification and denitrification process, and the surplus C5
5 fH (approximately 2%) and DAM-based (poly-dialkylamino-ethyl methacrylate-based) kaon polymer.
After adding 0% to SS to form flocs, it was dehydrated using a roll press type dehydrator [Ebara Infilco Product Deby Roll], and moisture containing calcium phosphate was 7.
A dewatered cake with a low moisture content of 2-74% was obtained, and the dewatered separation water was recycled to the reaeration tank.
以上述べたように本発明によれば、次のような重要な効
果を得ることができ、前記従来プロセスの問題点を完全
に解決することができる。As described above, according to the present invention, the following important effects can be obtained, and the problems of the conventional process can be completely solved.
■ 膜透過水のｐｏ、’−濃度を極めて低濃度にするこ
とができるので、従来プロセスのように膜透過水の高濃
度ＰＯ４トを除去するためのリン吸着工程を設ける必要
が全（ない。この結果プロセス構成が著しく簡略化され
、建設費は節減され、維持管理費も低減する。(2) Since the po,'-concentration of the membrane-permeated water can be made extremely low, there is no need to provide a phosphorus adsorption step to remove the high-concentration PO4 of the membrane-permeated water, as in conventional processes. As a result, the process configuration is significantly simplified, construction costs are reduced, and maintenance costs are also reduced.
■ 難濃縮脱水性のアルミニウム系又は鉄系スラフジが
発生しないのでｔｒ：泥処理が容易になる。■ Since aluminum-based or iron-based sludge, which is difficult to concentrate and dehydrate, is not generated, tr: mud treatment becomes easy.
■ 脱水ケーキ中に肥料としての価値が高いリン酸カル
シウムが豊富に含まれている。■ The dehydrated cake is rich in calcium phosphate, which has high value as a fertilizer.
■ 膜透過水に対するリン吸着工程が不要になるので、
当然吸着剤の再生、再生廃液の処分も不要になる。従来
プロセスで最も繁雑であった工程は、このリン吸着剤の
再生、再生廃液の処分であったので、本発明の効果は特
記される。■ Phosphorus adsorption process for membrane-permeated water is no longer necessary, so
Naturally, there is no need to regenerate the adsorbent or dispose of the regenerated waste liquid. The most complicated steps in the conventional process were the regeneration of the phosphorus adsorbent and the disposal of the regenerated waste liquid, so the effects of the present invention are noteworthy.
第１図は本発明の一実施態様を示すフローシートである
。
■・・・し尿、２・・・スクリーン、３・・・除渣し尿
、４・・・生物学的硝化脱窒素工程、５・・・第１脱窒
素槽、６・・・硝化槽、７・・・第２脱窒素槽、８・・
・カルシウムイオン源、９・・・再曝気槽、ｌＯ・・・
膜分離工程、１１・・・膜透過水、１２・・・膜分離ス
ラリ、１３・・・返送汚泥、１４・・・余剰汚泥、１５
・・・ｔη泥脱水工程、１６・・・脱水ケーキ、１７・
・・脱水分離水。FIG. 1 is a flow sheet showing one embodiment of the present invention. ■... Human waste, 2... Screen, 3... Sediment removal human waste, 4... Biological nitrification and denitrification process, 5... First denitrification tank, 6... Nitrification tank, 7 ...Second denitrification tank, 8...
・Calcium ion source, 9...reaeration tank, lO...
Membrane separation step, 11... Membrane permeated water, 12... Membrane separation slurry, 13... Returned sludge, 14... Excess sludge, 15
...tη mud dewatering process, 16... dehydrated cake, 17.
...Dehydrated and separated water.
Claims (1)
化脱窒素工程で処理する方法において、ＢＯＤ、窒素成
分の少なくとも大部分を除去し、カルシウムイオンの共
存下で該微生物スラリを水温３０〜４５℃、ｐＨ７．５
〜９．５の条件下に維持したのち膜分離し、分離された
膜分離スラリを前記生物学的硝化脱窒素工程に返送する
ことを特徴とする有機性汚水の処理方法。(1) In a method of treating organic wastewater containing phosphorus and nitrogen components through a biological nitrification and denitrification process, BOD and at least most of the nitrogen components are removed, and the microbial slurry is processed at a water temperature of 30°C in the coexistence of calcium ions. ~45℃, pH7.5
A method for treating organic wastewater, which comprises maintaining the organic wastewater under the conditions of 9.5, performing membrane separation, and returning the separated membrane-separated slurry to the biological nitrification and denitrification process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62138986A JPS63302996A (en) | 1987-06-04 | 1987-06-04 | Treatment of organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62138986A JPS63302996A (en) | 1987-06-04 | 1987-06-04 | Treatment of organic sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63302996A true JPS63302996A (en) | 1988-12-09 |
| JPH0325239B2 JPH0325239B2 (en) | 1991-04-05 |
Family
ID=15234810
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62138986A Granted JPS63302996A (en) | 1987-06-04 | 1987-06-04 | Treatment of organic sewage |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63302996A (en) |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03114597A (en) * | 1989-09-29 | 1991-05-15 | Sumitomo Jukikai Envirotec Kk | Method for controlling biological denitrification |
| EP0509152A1 (en) * | 1991-04-17 | 1992-10-21 | Ecotechniek B.V. | Method and apparatus for processing manure |
| US5296147A (en) * | 1989-10-17 | 1994-03-22 | Ecotechniek B.V. | Method for processing manure, fermented manure and ammonium nitrogen containing waste water |
| WO1997037942A1 (en) * | 1996-04-10 | 1997-10-16 | Herhof Umwelttechnik Gmbh | Process and device for treatment of water from a biodegradeable process |
| US6406629B1 (en) | 1999-07-20 | 2002-06-18 | Zenon Environmental Inc. | Biological process for removing phosphorous involving a membrane filter |
| US6485645B1 (en) | 1999-07-20 | 2002-11-26 | Zenon Environmental Inc | Biological process for removing phosphorus involving a membrane filter |
| WO2003002468A1 (en) * | 2001-06-28 | 2003-01-09 | Zenon Environmental Inc. | A process for reducing concentrations of hair, trash, or fibrous materials in a waste water |
| WO2003057632A1 (en) * | 2002-01-07 | 2003-07-17 | Berliner Wasser Betriebe | Biological treatment process involving post-denitrification mechanism and a membrane filter |
| US6814868B2 (en) | 2001-06-28 | 2004-11-09 | Zenon Environmental Inc. | Process for reducing concentrations of hair, trash, or fibrous materials, in a waste water treatment system |
| JP2005007257A (en) * | 2003-06-18 | 2005-01-13 | Ataka Construction & Engineering Co Ltd | Phosphorus recovering apparatus and method for treating phosphorus-containing organic wastewater |
| US7344643B2 (en) | 2005-06-30 | 2008-03-18 | Siemens Water Technologies Holding Corp. | Process to enhance phosphorus removal for activated sludge wastewater treatment systems |
| JP2008188498A (en) * | 2007-02-01 | 2008-08-21 | Kobelco Eco-Solutions Co Ltd | Treatment method and treatment equipment for treated water |
| US7473364B2 (en) | 2006-03-07 | 2009-01-06 | Siemens Water Technologies Corp. | Multivalent metal ion management for low sludge processes |
| US7569147B2 (en) | 2005-09-02 | 2009-08-04 | Siemens Water Technologies Corp. | Screening of inert solids from a low-yield wastewater treatment process |
| EP1807361A4 (en) * | 2004-08-26 | 2009-12-02 | Carollo Engineers Pc | SYSTEM AND METHOD FOR ANOXIC BIOLOGICAL REDUCTION |
| US8894856B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US8894855B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US8894857B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Methods and systems for treating wastewater |
| US9359236B2 (en) | 2010-08-18 | 2016-06-07 | Evoqua Water Technologies Llc | Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle |
| US10131550B2 (en) | 2013-05-06 | 2018-11-20 | Evoqua Water Technologies Llc | Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS565192A (en) * | 1979-06-28 | 1981-01-20 | Ebara Infilco Co Ltd | Highly advanced treatment of waste water |
| JPS61287499A (en) * | 1985-06-12 | 1986-12-17 | Kubota Ltd | Treatment of organic sewage |
-
1987
- 1987-06-04 JP JP62138986A patent/JPS63302996A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS565192A (en) * | 1979-06-28 | 1981-01-20 | Ebara Infilco Co Ltd | Highly advanced treatment of waste water |
| JPS61287499A (en) * | 1985-06-12 | 1986-12-17 | Kubota Ltd | Treatment of organic sewage |
Cited By (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03114597A (en) * | 1989-09-29 | 1991-05-15 | Sumitomo Jukikai Envirotec Kk | Method for controlling biological denitrification |
| US5296147A (en) * | 1989-10-17 | 1994-03-22 | Ecotechniek B.V. | Method for processing manure, fermented manure and ammonium nitrogen containing waste water |
| EP0509152A1 (en) * | 1991-04-17 | 1992-10-21 | Ecotechniek B.V. | Method and apparatus for processing manure |
| US5290451A (en) * | 1991-04-17 | 1994-03-01 | Ecotechniek B.V. | Method and apparatus for processing manure |
| WO1997037942A1 (en) * | 1996-04-10 | 1997-10-16 | Herhof Umwelttechnik Gmbh | Process and device for treatment of water from a biodegradeable process |
| US6113787A (en) * | 1996-04-10 | 2000-09-05 | Herhof Umwelttechnik Gmbh | Process and device for treatment of water from a biodegradeable process |
| US6406629B1 (en) | 1999-07-20 | 2002-06-18 | Zenon Environmental Inc. | Biological process for removing phosphorous involving a membrane filter |
| US6485645B1 (en) | 1999-07-20 | 2002-11-26 | Zenon Environmental Inc | Biological process for removing phosphorus involving a membrane filter |
| WO2003002468A1 (en) * | 2001-06-28 | 2003-01-09 | Zenon Environmental Inc. | A process for reducing concentrations of hair, trash, or fibrous materials in a waste water |
| US6814868B2 (en) | 2001-06-28 | 2004-11-09 | Zenon Environmental Inc. | Process for reducing concentrations of hair, trash, or fibrous materials, in a waste water treatment system |
| WO2003057632A1 (en) * | 2002-01-07 | 2003-07-17 | Berliner Wasser Betriebe | Biological treatment process involving post-denitrification mechanism and a membrane filter |
| JP2005007257A (en) * | 2003-06-18 | 2005-01-13 | Ataka Construction & Engineering Co Ltd | Phosphorus recovering apparatus and method for treating phosphorus-containing organic wastewater |
| EP1807361A4 (en) * | 2004-08-26 | 2009-12-02 | Carollo Engineers Pc | SYSTEM AND METHOD FOR ANOXIC BIOLOGICAL REDUCTION |
| US7344643B2 (en) | 2005-06-30 | 2008-03-18 | Siemens Water Technologies Holding Corp. | Process to enhance phosphorus removal for activated sludge wastewater treatment systems |
| US7569147B2 (en) | 2005-09-02 | 2009-08-04 | Siemens Water Technologies Corp. | Screening of inert solids from a low-yield wastewater treatment process |
| US7473364B2 (en) | 2006-03-07 | 2009-01-06 | Siemens Water Technologies Corp. | Multivalent metal ion management for low sludge processes |
| JP2008188498A (en) * | 2007-02-01 | 2008-08-21 | Kobelco Eco-Solutions Co Ltd | Treatment method and treatment equipment for treated water |
| US8894856B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US8894855B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US8894857B2 (en) | 2008-03-28 | 2014-11-25 | Evoqua Water Technologies Llc | Methods and systems for treating wastewater |
| US9359239B2 (en) | 2008-03-28 | 2016-06-07 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US9359238B2 (en) | 2008-03-28 | 2016-06-07 | Evoqua Water Technologies Llc | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods |
| US9359236B2 (en) | 2010-08-18 | 2016-06-07 | Evoqua Water Technologies Llc | Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle |
| US9783440B2 (en) | 2010-08-18 | 2017-10-10 | Evoqua Water Technologies Llc | Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle |
| US10131550B2 (en) | 2013-05-06 | 2018-11-20 | Evoqua Water Technologies Llc | Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0325239B2 (en) | 1991-04-05 |
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