JPH10277543A - Method for nitrification and denitrification of nitrogen-containing waste water - Google Patents
Method for nitrification and denitrification of nitrogen-containing waste waterInfo
- Publication number
- JPH10277543A JPH10277543A JP9053697A JP9053697A JPH10277543A JP H10277543 A JPH10277543 A JP H10277543A JP 9053697 A JP9053697 A JP 9053697A JP 9053697 A JP9053697 A JP 9053697A JP H10277543 A JPH10277543 A JP H10277543A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- zeolite
- carrier
- denitrification
- nitrification
- 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
- 238000000034 method Methods 0.000 title claims description 26
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 title claims description 18
- 239000002351 wastewater Substances 0.000 title claims description 18
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 56
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000010457 zeolite Substances 0.000 claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000005273 aeration Methods 0.000 claims abstract description 14
- 230000005484 gravity Effects 0.000 claims abstract description 13
- 239000004372 Polyvinyl alcohol Substances 0.000 claims abstract description 5
- 229920002451 polyvinyl alcohol Polymers 0.000 claims abstract description 5
- 238000001179 sorption measurement Methods 0.000 claims description 38
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- 230000001546 nitrifying effect Effects 0.000 claims description 6
- -1 polypropylene Polymers 0.000 claims description 6
- 239000004677 Nylon Substances 0.000 claims description 3
- 239000004698 Polyethylene Substances 0.000 claims description 3
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 229920001778 nylon Polymers 0.000 claims description 3
- 229920000573 polyethylene Polymers 0.000 claims description 3
- 229920000306 polymethylpentene Polymers 0.000 claims description 3
- 239000011116 polymethylpentene Substances 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 18
- 239000000126 substance Substances 0.000 abstract description 5
- 239000011248 coating agent Substances 0.000 abstract 1
- 238000000576 coating method Methods 0.000 abstract 1
- 239000010802 sludge Substances 0.000 description 13
- 238000004062 sedimentation Methods 0.000 description 7
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 6
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Water Treatment By Sorption (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、下水等のような窒
素含有排水の改良された脱窒方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an improved method for denitrification of nitrogen-containing wastewater such as sewage.
【０００２】[0002]
【従来の技術】従来、下水等のような窒素含有排水の脱
窒方法には、通常、図５に例示するような硝化液循環法
が用いられている。この方法では、先ず脱窒槽１１で主
として硝化液中の亜硝酸態および硝酸態の窒素分がＮ2
ガスとして取り出されるが、分解されなかった原水中の
窒素含有物を次の硝化槽１２において亜硝酸態および硝
酸態に酸化分解して、先の脱窒槽１１に返送、循環する
ようにして、排水中の有機物を利用して脱窒した後、沈
殿槽１４で汚泥を分離し、処理水とされる。このとき、
沈殿槽１４から抜き出された汚泥の一部は、返送汚泥と
して先頭の脱窒槽１１に送り返される。2. Description of the Related Art Conventionally, as a method for denitrifying nitrogen-containing wastewater such as sewage, a nitrification liquid circulation method as illustrated in FIG. 5 is usually used. In this method, first, in the denitrification tank 11, the nitrogen content of nitrite and nitrate in the nitrification liquid is reduced to N 2
The nitrogen-containing material in the raw water which is taken out as a gas but not decomposed is oxidized and decomposed into nitrite and nitrate in the next nitrification tank 12, returned to the denitrification tank 11 and circulated, and drained. After denitrification using the organic matter in the sludge, the sludge is separated in the sedimentation tank 14 and used as treated water. At this time,
Part of the sludge extracted from the sedimentation tank 14 is returned to the head denitrification tank 11 as returned sludge.
【０００３】この場合の脱窒率は、硝化液の循環率で決
定されるので、脱窒効果を高めようとすれば、その循環
率を増加させる必要があるが、そのためには硝化液を循
環させるためのポンプなどの動力が増加するほか、脱窒
槽の容量を拡大しなければ対応できないという問題があ
った。[0003] In this case, the denitrification rate is determined by the circulation rate of the nitrification liquid. Therefore, in order to enhance the denitrification effect, it is necessary to increase the circulation rate. In addition to increasing the power of pumps and the like, there was a problem that it was not possible to cope without increasing the capacity of the denitrification tank.
【０００４】また、脱窒率を高める方法として、図６に
例示するようなメタノール添加法も実用化されている。
この方法では、反応槽として、硝化槽１２、脱窒槽１
１、および再曝気槽１３を配列して、硝化槽１２におい
ては原水を曝気して窒素含有物を亜硝酸態および硝酸態
に酸化分解し、次いで脱窒槽１１では、メタノールを添
加しながら亜硝酸態および硝酸態窒素をＮ2 ガスに分解
し除去するのであるが、相当量のメタノールを消費する
ので、下水のように処理量が大量になる場合の処理方法
としては適当ではなかった。As a method for increasing the denitrification rate, a methanol addition method as illustrated in FIG. 6 has been put to practical use.
In this method, as a reaction tank, a nitrification tank 12, a denitrification tank 1
1, a re-aeration tank 13 is arranged, and in a nitrification tank 12, raw water is aerated to oxidize and decompose nitrogen-containing substances into nitrite and nitrate forms. Then, in a denitrification tank 11, nitrite is added while methanol is added. It decomposes and removes nitrogen and nitrate into N 2 gas, but consumes a considerable amount of methanol, and is not suitable as a treatment method when the treatment amount is large, such as sewage.
【０００５】[0005]
【発明が解決しようとする課題】本発明は、上記の問題
点を解決するためになされたものであり、脱窒率の向上
を企図する脱窒方法であり、メタノールのような添加薬
品を必要とせず、設備を比較的コンパクトに構成するこ
とが可能となる窒素含有排水の脱窒方法を提供する。SUMMARY OF THE INVENTION The present invention has been made to solve the above problems, and is a denitrification method intended to improve the denitrification rate, and requires an additive chemical such as methanol. The present invention provides a method for denitrifying nitrogen-containing wastewater, which makes it possible to make the equipment relatively compact.
【０００６】[0006]
【課題を解決するための手段】上記の問題は、窒素含有
排水をゼオライト吸着槽、硝化槽、脱窒槽、および再曝
気槽にて処理して窒素分を除去する方法であって、ゼオ
ライト吸着槽と硝化槽と脱窒槽にゼオライト担持担体を
添加し、ゼオライト吸着槽において排水中のアンモニア
性窒素を吸着分離させ、硝化槽において硝化した後に、
脱窒槽においてその硝化液を脱窒するに際して、前記ゼ
オライト吸着槽からアンモニア性窒素を吸着分離させた
排水を取り出して脱窒槽に送り込み、前記硝化液に混合
して脱窒反応を行うとともに、脱窒槽からゼオライト担
持担体を取り出してゼオライト吸着槽に返送して、ゼオ
ライト吸着槽と脱窒槽の間を循環させるこを特徴とする
窒素含有排水の硝化脱窒方法により解決することができ
る。An object of the present invention is to provide a method for removing nitrogen by treating nitrogen-containing wastewater in a zeolite adsorption tank, a nitrification tank, a denitrification tank, and a re-aeration tank. After adding the zeolite-supported carrier to the nitrification tank and the denitrification tank, the ammonia nitrogen in the wastewater is adsorbed and separated in the zeolite adsorption tank, and after nitrification in the nitrification tank,
When denitrifying the nitrification liquid in the denitrification tank, the drainage from which the ammonia nitrogen was adsorbed and separated from the zeolite adsorption tank was taken out, sent to the denitrification tank, mixed with the nitrification liquid to perform the denitrification reaction, and The method can be solved by a method for nitrifying and denitrifying nitrogen-containing wastewater, which comprises taking out a zeolite-supporting carrier from the reactor and returning it to a zeolite adsorption tank and circulating it between the zeolite adsorption tank and the denitrification tank.
【０００７】また、本発明は、前記ゼオライト担持担体
として、ポリビニルアルコールからなり比重が１．０５
〜１．３０の範囲の担体に、粉状合成ゼオライトを被覆
した担体、または粉状合成ゼオライトを内部に包括固定
した担体を使用するとともに、脱窒槽からエアリフトポ
ンプを用いて取り出し、ゼオライト吸着槽に返送する形
態の窒素含有排水の硝化脱窒方法として、具体化するこ
とができる。In the present invention, the zeolite-supporting carrier comprises polyvinyl alcohol and has a specific gravity of 1.05.
A carrier coated with powdery synthetic zeolite or a carrier in which powdery synthetic zeolite is wrapped and fixed inside a carrier in the range of ~ 1.30, taken out from the denitrification tank using an air lift pump, and put into a zeolite adsorption tank It can be embodied as a method for nitrifying and denitrifying nitrogen-containing wastewater in a form to be returned.
【０００８】さらに、本発明は、前記ゼオライト担持担
体として、発泡ポリプロピレン、発泡ポリエチレン、発
泡ポリメチルペンテン、または発泡ナイロンからなり比
重が０．９５〜０．９９の範囲の担体に粉状合成ゼオラ
イトを担持した担体を使用するとともに、脱窒槽からベ
ルトコンベヤまたはフライトコンベヤを用いて取り出
し、ゼオライト吸着槽に返送する形態の窒素含有排水の
硝化脱窒方法としても、具体化することができる。Further, the present invention provides a method for preparing a zeolite-supported carrier comprising powdered synthetic zeolite on a carrier made of expanded polypropylene, expanded polyethylene, expanded polymethylpentene, or expanded nylon having a specific gravity of 0.95 to 0.99. A method for nitrifying and denitrifying nitrogen-containing wastewater, in which a supported carrier is used and taken out from a denitrification tank using a belt conveyor or a flight conveyor and returned to a zeolite adsorption tank, can be embodied.
【０００９】[0009]
【発明の実施の形態】次に、本発明の実施形態につい
て、図１、２を参照して説明する。この実施形態では、
窒素含有排水である原水から含有窒素分を除去するため
の反応槽としては、ゼオライト吸着槽２、硝化槽３、脱
窒槽４、および再曝気槽５を用いる。この除去反応の
後、沈殿槽６にて汚泥を沈澱分離した処理水が排出さ
れ、抜き出された汚泥の一部は、先の硝化槽３へ返送汚
泥として戻され、他は余剰汚泥として排出される。Next, an embodiment of the present invention will be described with reference to FIGS. In this embodiment,
A zeolite adsorption tank 2, a nitrification tank 3, a denitrification tank 4, and a re-aeration tank 5 are used as reaction tanks for removing nitrogen content from raw water that is nitrogen-containing waste water. After this removal reaction, the treated water obtained by sedimentation and separation of the sludge in the sedimentation tank 6 is discharged, and a part of the extracted sludge is returned to the previous nitrification tank 3 as returned sludge, and the other is discharged as surplus sludge. Is done.
【００１０】本発明では、このように各反応槽の順に原
水が処理されるのであるが、先ず、先頭のゼオライト吸
着槽２には、導入された原水に含まれるアンモニア性窒
素を吸着するためのゼオライト担持担体が添加してあ
る。このゼオライト担持担体としては、図１の場合のよ
うに、ポリビニルアルコールからなり比重が１．０５〜
１．３０の範囲の担体に粉状合成ゼオライトを被覆した
担体、または粉状合成ゼオライトを内部に包括固定した
担体のように、比較的比重の重い担体が使用されるが、
その他にも、図２の場合のように、発泡ポリプロピレ
ン、発泡ポリエチレン、発泡ポリメチルペンテン、また
は発泡ナイロンからなり比重が０．９５〜０．９９の範
囲の担体に粉状合成ゼオライトを担持した担体のよう
に、比較的比重の軽い担体も同様に使用することができ
る。In the present invention, raw water is treated in the order of each reaction tank as described above. First, the leading zeolite adsorption tank 2 is used to adsorb ammonia nitrogen contained in the introduced raw water. A zeolite-supported carrier has been added. This zeolite-supporting carrier is made of polyvinyl alcohol and has a specific gravity of 1.05 to 1.0 as shown in FIG.
A carrier having a relatively heavy specific gravity is used, such as a carrier in which powdery synthetic zeolite is coated on a carrier in the range of 1.30 or a carrier in which powdery synthetic zeolite is encapsulated and fixed.
In addition, as shown in FIG. 2, a carrier made of expanded polypropylene, expanded polyethylene, expanded polymethylpentene, or expanded nylon, and having a specific gravity in the range of 0.95 to 0.99, on which a powdery synthetic zeolite is supported As described above, a carrier having a relatively low specific gravity can be used as well.
【００１１】図１の事例は、前記の比重の重いゼオライ
ト担持担体を使用した場合を例示するものである。ここ
で、ゼオライト吸着槽２に導入された原水に含まれるア
ンモニア性窒素は、予め添加されていたゼオライト担持
担体に選択的に吸着されるが、このゼオライト担持担体
は、アンモニア性窒素を伴って、次の硝化槽３に流入し
て、硝化反応によりアンモニア性窒素は亜硝酸態または
硝酸態窒素に変化して、ゼオライト担持担体から遊離す
る。これらは、さらに脱窒槽４に流入して脱窒されるの
である。一方、ゼオライト吸着槽２において、アンモニ
ア性窒素を分離したものの、その他有機物を含む原水
は、後半部分に設けられたポンプ２１で汲み上げられ、
後段の脱窒槽４の前半部分に直接に送り込まれる。この
場合、スクリーン２２により担体はポンプ側に流入しな
いよう隔てられている。そして、この脱窒槽４におい
て、硝化槽３から流入してきた亜硝酸態または硝酸態窒
素を含む硝化液と混合され、この原水中の有機物を利用
して脱窒反応が促進されることになる。FIG. 1 illustrates the case where the above-mentioned zeolite-supported carrier having a high specific gravity is used. Here, the ammonia nitrogen contained in the raw water introduced into the zeolite adsorption tank 2 is selectively adsorbed on the zeolite-supporting carrier that has been added in advance. After flowing into the next nitrification tank 3, the ammoniacal nitrogen is changed to nitrite or nitrate nitrogen by the nitrification reaction and released from the zeolite-supporting carrier. These further flow into the denitrification tank 4 and are denitrified. On the other hand, in the zeolite adsorption tank 2, although the ammonia nitrogen is separated, the raw water containing other organic substances is pumped by the pump 21 provided in the latter half part,
It is sent directly to the first half of the denitrification tank 4 in the latter stage. In this case, the carrier is separated by the screen 22 so as not to flow into the pump side. Then, in the denitrification tank 4, the denitrification reaction is promoted by mixing with the nitrification liquid containing nitrite or nitrate nitrogen flowing from the nitrification tank 3 and utilizing the organic matter in the raw water.
【００１２】このように、硝化槽３において、ゼオライ
ト担持担体に吸着していたアンモニア性窒素は硝化反応
により変化して離脱するので、ゼオライト担持担体の吸
着機能が再生する。そして、完全に吸着機能が再生した
ゼオライト担持担体は、次の脱窒槽４の後半部分に設け
られているエアリフトポンプ４１で汲み上げられ返送パ
イプ４２を通って、先のゼオライト吸着槽２の前半部分
に返送される。なお、ゼオライト吸着槽２から直接に送
られてきた原水中の有機性窒素が脱窒槽４において、ア
ンモニア性窒素に変化したときには、このアンモニア性
窒素をゼオライト担持担体が吸着した状態で、ゼオライ
ト吸着槽２へ返送されるので、アンモニア性窒素が後段
の再曝気槽５へ流出することはない。As described above, in the nitrification tank 3, the ammonia nitrogen adsorbed on the zeolite-supported carrier is changed and desorbed by the nitrification reaction, so that the adsorption function of the zeolite-supported carrier is regenerated. The zeolite-supported carrier whose adsorption function has been completely regenerated is pumped up by the air lift pump 41 provided in the second half of the next denitrification tank 4 and passes through the return pipe 42 to the first half of the previous zeolite adsorption tank 2. Will be returned. When the organic nitrogen in the raw water sent directly from the zeolite adsorption tank 2 is changed to ammonia nitrogen in the denitrification tank 4, the ammonia nitrogen is absorbed by the zeolite-supporting carrier in the zeolite adsorption tank. Since it is returned to 2, the ammonia nitrogen does not flow out to the rear-stage aeration tank 5.
【００１３】そして、本発明では、ゼオライト担持担体
が、このように原水に含まれるアンモニア性窒素を吸着
して、硝化、脱窒という順に処理が行われ、さらに脱窒
槽４からゼオライト吸着槽２に返送されるというよう
に、ゼオライト担持担体が、原水中のアンモニア性窒素
および脱窒反応で生じるアンモニア性窒素を吸着して、
硝化反応を特に促進するという好ましい循環が行われる
のである。In the present invention, the zeolite-supporting carrier adsorbs the ammonia nitrogen contained in the raw water as described above, and is treated in the order of nitrification and denitrification. As it is returned, the zeolite-supported carrier adsorbs the ammonia nitrogen in the raw water and the ammonia nitrogen generated by the denitrification reaction,
A favorable circulation is performed in which the nitrification reaction is particularly accelerated.
【００１４】この図１に示される実施形態で用いられる
ゼオライト担持担体は、ポリビニルアルコールからなり
比重が１．０１〜１．０５程度の担体であり、その組織
は極めて脆弱であるところから、その移送に当たっては
空気泡の上昇流を利用したエアリフトポンプ４１を応用
するのが好ましく、また、ゼオライト吸着槽２、硝化槽
３、脱窒槽４の各境界の流通開口は、ゼオライト担持担
体の流通を阻害しないような大きさで、適宜な深さに設
ければよい。また、必要に応じて、脱窒槽４と再曝気槽
５との境界には、図２に示すようなスクリーン４４を設
け、ゼオライト担持担体の流通を阻止するように構成し
てもよい。The zeolite-supporting carrier used in the embodiment shown in FIG. 1 is a carrier made of polyvinyl alcohol and having a specific gravity of about 1.01 to 1.05, and its tissue is extremely fragile. In this case, it is preferable to apply an air lift pump 41 utilizing the upward flow of air bubbles, and the flow openings at the boundaries of the zeolite adsorption tank 2, the nitrification tank 3, and the denitrification tank 4 do not hinder the flow of the zeolite-supporting carrier. What is necessary is just to provide in such a magnitude | size and the appropriate depth. If necessary, a screen 44 as shown in FIG. 2 may be provided at the boundary between the denitrification tank 4 and the re-aeration tank 5 so as to block the flow of the zeolite carrier.
【００１５】この実施形態における諸元を例示すると、
ゼオライト担持担体の各反応槽に対する添加量は５〜３
０ｖｏｌ％、その循環率は２０〜４０％程度がよい。ま
た、各反応槽での処理時間（滞留時間）は、ゼオライト
吸着槽が約０．５〜１時間、硝化槽が約１〜３時間（硝
化速度４〜７ｋｇN ／ｍ3 担体）、脱窒槽が約２〜５時
間（脱窒速度２．５〜３ｋｇN ／ｍ3 担体）、および再
曝気槽が約２〜３時間でよい。また、活性汚泥の濃度
は、活性汚泥法並みの５００〜３０００ｍｇ／ｌ程度で
よい。The specifications of this embodiment are as follows.
The amount of the zeolite-supported carrier added to each reaction tank is 5 to 3
0 vol%, and its circulation rate is preferably about 20 to 40%. The treatment time (residence time) in each reaction tank is about 0.5 to 1 hour in the zeolite adsorption tank, about 1 to 3 hours in the nitrification tank (nitrification rate 4 to 7 kgN / m 3 carrier), and the denitrification tank is About 2 to 5 hours (denitrification rate 2.5 to 3 kgN / m 3 carrier), and the re-aeration tank may be about 2 to 3 hours. The concentration of the activated sludge may be about 500 to 3000 mg / l, which is equivalent to the activated sludge method.
【００１６】次に本発明による２、３の特性について説
明すると、先ず、図３は、原水のアンモニア性窒素が２
５ｍｇ／ｌの場合のゼオライト吸着槽の滞留時間とアン
モニア性窒素の除去率の関係を担体添加率をパラメータ
にして示したグラフであり、これによれば、ゼオライト
担持担体の添加率が１０〜３０ｖｏｌ％であるときのゼ
オライト吸着槽２の滞留時間は０．５時間でよく、また
５ｖｏｌ％のときでも１時間の滞留時間で充分であるこ
とが分かる。Next, a description will be given of a few characteristics according to the present invention. First, FIG.
5 is a graph showing the relationship between the residence time of the zeolite adsorption tank and the removal rate of ammonia nitrogen in the case of 5 mg / l, using the carrier addition rate as a parameter, according to which the addition rate of the zeolite-supported carrier is 10 to 30 vol. %, The residence time of the zeolite adsorption tank 2 may be 0.5 hour, and it can be seen that a residence time of 1 hour is sufficient even at 5 vol%.
【００１７】また、図４は、担体添加量に対する担体循
環率の比率（倍）と循環担体濃度（ｖｏｌ％）およびＴ
−Ｎ除去率の関係を、担体添加率１０ｖｏｌ％の場合に
ついて示したグラフである。これによると、Ｔ−Ｎ除去
率は、担体添加量に対する担体循環率の比率が１〜４倍
のとき、７５〜８５％の高い値が得られる。一方、循環
担体の濃度は、担体添加量に対する担体循環率の比率が
１．７倍以上のとき、６０ｖｏｌ％以下になって、硝化
槽３における担体の流動化が可能となり、硝化のための
曝気ができるようになる。従って、Ｔ−Ｎ除去率を７５
〜８５％の高いレベルに維持し、かつ硝化槽３における
担体の流動化を確保するためには、担体添加量に対する
担体循環率の比率として２〜４倍が好ましいことが分か
る。例えば、図の場合、原水に対する担体添加率（反応
槽容積に対する担体添加量）は１０ｖｏｌ％であるか
ら、担体の循環率を原水の２０〜４０ｖｏｌ％に設定す
れば、硝化槽３における担体の流動化が可能になるとと
もに、Ｔ−Ｎ除去率を７５〜８５％程度にすることがで
きるのである。FIG. 4 shows the ratio (times) of the carrier circulation rate to the carrier addition amount, the circulating carrier concentration (vol%), and T
It is the graph which showed the relationship of -N removal rate about the case of 10 vol% of carrier addition rates. According to this, a high value of 75 to 85% is obtained for the TN removal rate when the ratio of the carrier circulation rate to the carrier addition amount is 1 to 4 times. On the other hand, when the ratio of the carrier circulation rate to the carrier addition amount is 1.7 times or more, the concentration of the circulating carrier becomes 60 vol% or less, and the fluidization of the carrier in the nitrification tank 3 becomes possible, and aeration for nitrification is performed. Will be able to Therefore, the TN removal rate is 75
It can be seen that the ratio of the carrier circulation rate to the carrier addition amount is preferably 2 to 4 times in order to maintain the carrier at a high level of ~ 85% and to ensure the fluidization of the carrier in the nitrification tank 3. For example, in the case of the figure, since the carrier addition rate to the raw water (the carrier addition amount to the reaction tank volume) is 10 vol%, if the circulation rate of the carrier is set to 20 to 40 vol%, the carrier flow in the nitrification tank 3 This makes it possible to reduce the TN removal rate to about 75 to 85%.
【００１８】なお、この実施形態では、脱窒槽４の後段
に設けられている再曝気槽４は、散気装置から空気が送
り込まれて好気状態を保持して、残余の有機物を分解す
るためのものである。また、沈澱槽６から抜き出された
汚泥の一部は、先の硝化槽３へ返送汚泥として戻されて
いるが、これを先頭のゼオライト吸着槽２へ返送するよ
うにしてもよく、その場合には、原水中のリン分の除去
も可能とすることができる。In this embodiment, the re-aeration tank 4 provided at the subsequent stage of the denitrification tank 4 is used to decompose the remaining organic matter while maintaining the aerobic state by the air being supplied from the air diffuser. belongs to. A part of the sludge extracted from the sedimentation tank 6 is returned to the previous nitrification tank 3 as returned sludge. However, this may be returned to the head zeolite adsorption tank 2. In addition, the removal of the phosphorus content in the raw water can be made possible.
【００１９】次に、図２を参照して、前記の比重の軽い
０．９５〜０．９９程度のゼオライト担持担体を使用し
た場合の実施形態について説明する。この実施形態で
は、窒素含有排水から含有窒素分を除去するためのゼオ
ライト吸着槽２、硝化槽３、脱窒槽３、および再曝気槽
４を用い、沈殿槽６にて汚泥を沈澱分離した処理水を排
出するという基本的構成、また、ゼオライト担持担体の
ゼオライト吸着槽２から脱窒槽３に至るまでの作用、お
よびゼオライト吸着槽２において、アンモニア性窒素を
分離した原水をポンプ２１で汲み上げ、後段の脱窒槽４
に送り込む操作などにおいて、先の実施形態の場合と同
様である。Next, with reference to FIG. 2, an embodiment in which the zeolite-supported carrier having a low specific gravity of about 0.95 to 0.99 is used will be described. In this embodiment, treated water obtained by separating and separating sludge in a sedimentation tank 6 using a zeolite adsorption tank 2, a nitrification tank 3, a denitrification tank 3, and a re-aeration tank 4 for removing nitrogen content from nitrogen-containing wastewater. And the operation of the zeolite-supporting carrier from the zeolite adsorption tank 2 to the denitrification tank 3, and in the zeolite adsorption tank 2, raw water from which ammonia nitrogen has been separated is pumped up by the pump 21. Denitrification tank 4
And the like, are the same as in the previous embodiment.
【００２０】その相違点は、その脱窒槽４からゼオライ
ト担持担体を汲み上げてゼオライト吸着槽２へ返送する
のに、ベルトコンベヤまたはフライトコンベヤのような
コンベヤ４３を用いている点にある。この場合のゼオラ
イト担持担体は、その組織は比較的丈夫で形状を保持す
る性質があるうえ、比重が１以下であって被処理水の上
層に浮遊しやすいから、その移送にあたっては、前記の
ように、ベルトコンベヤまたはフライトコンベヤのよう
な形式のコンベヤを応用するのが好ましい。なお、脱窒
槽４と再曝気槽５との境界には、スクリーン４４を設け
てゼオライト担持担体が再曝気槽５側に流入するのを阻
止している。また、ゼオライト吸着槽２から原水を汲み
出すときに、スクリーン２２を設けて浮遊するゼオライ
ト担持担体の流入を阻止して、ポンプ２１で汲み出すの
が適当である。The difference is that a conveyor 43 such as a belt conveyor or a flight conveyor is used to pump the zeolite-supporting carrier from the denitrification tank 4 and return it to the zeolite adsorption tank 2. In this case, the zeolite-supporting carrier has a property that its tissue is relatively strong and has a property of maintaining its shape, and has a specific gravity of 1 or less and easily floats on the upper layer of the water to be treated. Preferably, a conveyor of the type such as a belt conveyor or a flight conveyor is applied. A screen 44 is provided at the boundary between the denitrification tank 4 and the re-aeration tank 5 to prevent the zeolite-supporting carrier from flowing into the re-aeration tank 5 side. When pumping raw water from the zeolite adsorption tank 2, it is appropriate to provide a screen 22 to prevent inflow of the floating zeolite-carrying carrier, and to pump the raw water with the pump 21.
【００２１】次に、この第２の実施形態に具体化された
本発明の処理効果を従来例と対比して表１、２に示す。
この結果によれば、本発明と比較例の処理容量は、同じ
１００ｍ3 ／日であり、またその処理時間は、比較例が
８時間、本発明がそれより短い６時間であるが、本発明
では、その処理水の性状は、Ｔ−Ｎ、ＮＯ3 −Ｎとも大
幅に改善されている他、Ｔ−Ｐも改善されたうえ、ＳＳ
も改善される傾向が認められたのである。Next, the processing effects of the present invention embodied in the second embodiment are shown in Tables 1 and 2 in comparison with the conventional example.
According to this result, the processing capacity of the present invention and the comparative example is the same 100 m 3 / day, and the processing time is 8 hours in the comparative example and 6 hours shorter in the present invention. Then, the properties of the treated water have been greatly improved for both TN and NO 3 -N, and the TP has been improved.
Also tended to improve.
【００２２】[0022]
【表１】 （注１）ゼオライト吸着槽への返送率（％） （注２）ゼオライト吸着槽、硝化槽および脱窒槽の各添加率（％）[Table 1] (Note 1) Return rate to zeolite adsorption tank (%) (Note 2) Addition rate of zeolite adsorption tank, nitrification tank and denitrification tank (%)
【００２３】[0023]
【表２】 （注）従来法および本発明の処理水の欄のかっこ内数値は除去率％を示す。[Table 2] (Note) The values in parentheses in the columns of the treated water of the conventional method and the present invention indicate removal rates%.
【００２４】[0024]
【発明の効果】本発明の窒素含有排水の硝化脱窒方法
は、以上に説明したように構成されているので、次に示
すような優れた効果がある。 （１）メタノールのような添加薬品を必要とせず、含有
窒素を７５〜８５％の高率で除去することができる。 （２）担体により微生物の利用効率が向上し、硝化速度
を大きくすることができ、その結果硝化槽のコンパクト
化が可能となる。また、脱窒速度も大きくできるので脱
窒槽のコンパクト化も可能となる。 （３）担体に吸着されたアンモニア性窒素は硝化により
担体から遊離して、生物再生されるから、担体の耐用命
数が長くなる。 （４）原水の有機物に変動があっても、安定した脱窒が
可能である。 よって本発明は従来の問題点を解消した窒素含有排水の
硝化脱窒方法として、その工業的価値は極めて大なるも
のがある。The method for nitrifying and denitrifying nitrogen-containing waste water according to the present invention has the following excellent effects because it is configured as described above. (1) Nitrogen contained can be removed at a high rate of 75 to 85% without using an additive chemical such as methanol. (2) The use efficiency of microorganisms is improved by the carrier, and the nitrification rate can be increased. As a result, the nitrification tank can be made compact. Further, since the denitrification speed can be increased, the size of the denitrification tank can be reduced. (3) Since the ammonia nitrogen adsorbed on the carrier is released from the carrier by nitrification and is regenerated biologically, the useful life of the carrier becomes longer. (4) Stable denitrification is possible even if the organic matter in the raw water fluctuates. Therefore, the present invention has a very large industrial value as a method for nitrifying and denitrifying nitrogen-containing wastewater which has solved the conventional problems.
【図１】本発明の実施形態を説明するためのフロー図。FIG. 1 is a flowchart for explaining an embodiment of the present invention.
【図２】他の実施形態を説明するためのフロー図。FIG. 2 is a flowchart for explaining another embodiment.
【図３】本発明のゼオライト吸着槽滞留時間とＮＨ4 −
Ｎ除去率の関係を示すグラフ。FIG. 3 shows the retention time of the zeolite adsorption tank and NH 4 − of the present invention.
9 is a graph showing a relationship between N removal rates.
【図４】本発明の担体循環率とＴ−Ｎ除去率の関係を示
すグラフ。FIG. 4 is a graph showing the relationship between the carrier circulation rate and the TN removal rate according to the present invention.
【図５】従来の脱窒方法を説明するためのフロー図。FIG. 5 is a flowchart for explaining a conventional denitrification method.
【図６】他の従来の脱窒方法を説明するためのフロー
図。FIG. 6 is a flowchart for explaining another conventional denitrification method.
２ ゼオライト吸着槽、２１ ポンプ、３ 硝化槽、４
脱窒槽、４１ エアリフトポンプ、４２ 返送パイ
プ、５ 再曝気槽、６ 沈殿槽。2 zeolite adsorption tank, 21 pump, 3 nitrification tank, 4
Denitrification tank, 41 air lift pump, 42 return pipe, 5 re-aeration tank, 6 sedimentation tank.
Claims (3)
槽、脱窒槽、および再曝気槽にて処理して窒素分を除去
する方法であって、ゼオライト吸着槽と硝化槽と脱窒槽
にゼオライト担持担体を添加し、ゼオライト吸着槽にお
いて排水中のアンモニア性窒素を吸着分離させ、硝化槽
において硝化した後に、脱窒槽においてその硝化液を脱
窒するに際して、前記ゼオライト吸着槽からアンモニア
性窒素を吸着分離させた排水を取り出して脱窒槽に送り
込み、前記硝化液に混合して脱窒反応を行うとともに、
脱窒槽からゼオライト担持担体を取り出してゼオライト
吸着槽に返送して、ゼオライト吸着槽と脱窒槽の間を循
環させるこを特徴とする窒素含有排水の硝化脱窒方法。1. A method for removing nitrogen by treating nitrogen-containing wastewater in a zeolite adsorption tank, a nitrification tank, a denitrification tank, and a re-aeration tank, wherein the zeolite is loaded on the zeolite adsorption tank, the nitrification tank, and the denitrification tank. After adding a carrier, the ammonia nitrogen in the wastewater is adsorbed and separated in the zeolite adsorption tank, and after nitrification in the nitrification tank, when the nitrification liquid is denitrified in the denitrification tank, the ammonia nitrogen is adsorbed and separated from the zeolite adsorption tank. Take out the drained water and send it to a denitrification tank, and mix it with the nitrification solution to perform a denitrification reaction,
A method for nitrifying and denitrifying nitrogen-containing wastewater, comprising removing a zeolite-supporting carrier from a denitrification tank, returning the carrier to a zeolite adsorption tank, and circulating the carrier between the zeolite adsorption tank and the denitrification tank.
ニルアルコールからなり比重が１．０５〜１．３０の範
囲の担体に、粉状合成ゼオライトを被覆した担体、また
は粉状合成ゼオライトを内部に包括固定した担体を使用
するとともに、脱窒槽からエアリフトポンプを用いて取
り出し、ゼオライト吸着槽に返送する請求項１に記載の
窒素含有排水の脱窒方法。2. A zeolite-carrying carrier comprising polyvinyl alcohol and a specific gravity in the range of 1.05 to 1.30, wherein a carrier coated with powdery synthetic zeolite or a powdery synthetic zeolite is entrapped and fixed inside. The method for denitrifying nitrogen-containing wastewater according to claim 1, wherein the carrier is used, and the carrier is taken out of the denitrification tank using an air lift pump and returned to the zeolite adsorption tank.
リプロピレン、発泡ポリエチレン、発泡ポリメチルペン
テン、または発泡ナイロンからなり比重が０．９５〜
０．９９の範囲の担体に粉状合成ゼオライトを担持した
担体を使用するとともに、脱窒槽からベルトコンベヤま
たはフライトコンベヤを用いて取り出し、ゼオライト吸
着槽に返送する請求項１に記載の窒素含有排水の脱窒方
法。3. The zeolite-supporting carrier is made of expanded polypropylene, expanded polyethylene, expanded polymethylpentene, or expanded nylon, and has a specific gravity of 0.95 to 0.95.
The nitrogen-containing wastewater according to claim 1, wherein a carrier in which powdery synthetic zeolite is supported on a carrier having a range of 0.99 is used, and the carrier is taken out from the denitrification tank using a belt conveyor or a flight conveyor and returned to the zeolite adsorption tank. Denitrification method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09053697A JP3215349B2 (en) | 1997-04-09 | 1997-04-09 | Nitrification and denitrification of nitrogen-containing wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09053697A JP3215349B2 (en) | 1997-04-09 | 1997-04-09 | Nitrification and denitrification of nitrogen-containing wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH10277543A true JPH10277543A (en) | 1998-10-20 |
| JP3215349B2 JP3215349B2 (en) | 2001-10-02 |
Family
ID=14001147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP09053697A Expired - Fee Related JP3215349B2 (en) | 1997-04-09 | 1997-04-09 | Nitrification and denitrification of nitrogen-containing wastewater |
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| Country | Link |
|---|---|
| JP (1) | JP3215349B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100869058B1 (en) | 2008-03-28 | 2008-11-17 | (주)대성그린테크 | High concentration nitrogen containing industrial wastewater treatment method |
| KR101198334B1 (en) | 2011-07-07 | 2012-11-06 | 주식회사 성환이엔티 | Apparatus and Method for Treating Wastewater Using Zeolites Having Media |
| CN105883965A (en) * | 2016-05-13 | 2016-08-24 | 杭州启澄科技有限公司 | Cross-linked polyvininylpolyrrolidone supporter adsorption and purification system |
| CN107381958A (en) * | 2017-08-22 | 2017-11-24 | 轻工业环境保护研究所 | Carbon nitrogen divergence type denitrification process |
| CN109607984A (en) * | 2019-02-13 | 2019-04-12 | 轻工业环境保护研究所 | A high-concentration and high-nitrogen sewage treatment process |
| JP2019093329A (en) * | 2017-11-21 | 2019-06-20 | 清水建設株式会社 | Method of removing ammonia |
| JP2024013600A (en) * | 2022-07-20 | 2024-02-01 | 日本碍子株式会社 | Water treatment equipment, water treatment system, and method for recovering target substances |
-
1997
- 1997-04-09 JP JP09053697A patent/JP3215349B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100869058B1 (en) | 2008-03-28 | 2008-11-17 | (주)대성그린테크 | High concentration nitrogen containing industrial wastewater treatment method |
| KR101198334B1 (en) | 2011-07-07 | 2012-11-06 | 주식회사 성환이엔티 | Apparatus and Method for Treating Wastewater Using Zeolites Having Media |
| CN105883965A (en) * | 2016-05-13 | 2016-08-24 | 杭州启澄科技有限公司 | Cross-linked polyvininylpolyrrolidone supporter adsorption and purification system |
| CN107381958A (en) * | 2017-08-22 | 2017-11-24 | 轻工业环境保护研究所 | Carbon nitrogen divergence type denitrification process |
| JP2019093329A (en) * | 2017-11-21 | 2019-06-20 | 清水建設株式会社 | Method of removing ammonia |
| CN109607984A (en) * | 2019-02-13 | 2019-04-12 | 轻工业环境保护研究所 | A high-concentration and high-nitrogen sewage treatment process |
| JP2024013600A (en) * | 2022-07-20 | 2024-02-01 | 日本碍子株式会社 | Water treatment equipment, water treatment system, and method for recovering target substances |
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|---|---|
| JP3215349B2 (en) | 2001-10-02 |
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