JP6491056B2 - Nitrogen removal method and nitrogen removal apparatus - Google Patents
Nitrogen removal method and nitrogen removal apparatus Download PDFInfo
- Publication number
- JP6491056B2 JP6491056B2 JP2015136488A JP2015136488A JP6491056B2 JP 6491056 B2 JP6491056 B2 JP 6491056B2 JP 2015136488 A JP2015136488 A JP 2015136488A JP 2015136488 A JP2015136488 A JP 2015136488A JP 6491056 B2 JP6491056 B2 JP 6491056B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- nitrogen
- anaerobic
- biological treatment
- anoxic
- 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.)
- Active
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 142
- 238000000034 method Methods 0.000 title claims description 93
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 67
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 130
- 238000011282 treatment Methods 0.000 claims description 77
- 229910021529 ammonia Inorganic materials 0.000 claims description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- 239000010802 sludge Substances 0.000 claims description 37
- 230000003647 oxidation Effects 0.000 claims description 35
- 238000007254 oxidation reaction Methods 0.000 claims description 35
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 24
- 239000002351 wastewater Substances 0.000 claims description 24
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 18
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 16
- 229910017604 nitric acid Inorganic materials 0.000 claims description 16
- 230000029087 digestion Effects 0.000 claims description 15
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 12
- 230000001590 oxidative effect Effects 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 8
- 230000001546 nitrifying effect Effects 0.000 claims description 6
- 238000007667 floating Methods 0.000 claims description 4
- 238000005121 nitriding Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 description 41
- 239000007788 liquid Substances 0.000 description 36
- 241000894006 Bacteria Species 0.000 description 13
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 13
- 239000007787 solid Substances 0.000 description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 8
- 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 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 229910052698 phosphorus Inorganic materials 0.000 description 8
- 239000011574 phosphorus Substances 0.000 description 8
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000010865 sewage Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000005273 aeration Methods 0.000 description 6
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 5
- 238000000855 fermentation Methods 0.000 description 5
- 230000004151 fermentation Effects 0.000 description 5
- 241001453382 Nitrosomonadales Species 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- 230000001651 autotrophic effect Effects 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 238000013019 agitation Methods 0.000 description 3
- 239000000852 hydrogen donor Substances 0.000 description 3
- 235000015097 nutrients Nutrition 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 229910052588 hydroxylapatite Inorganic materials 0.000 description 2
- 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 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 229910052567 struvite Inorganic materials 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000001079 digestive effect Effects 0.000 description 1
- 239000000386 donor Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000003643 water by type 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Description
本発明は、窒素除去方法及び窒素除去装置に関し、特に、嫌気性アンモニア酸化法を用いて窒素含有廃水を処理する窒素除去方法及び窒素除去装置に関する。 The present invention relates to a nitrogen removal method and a nitrogen removal apparatus, and more particularly to a nitrogen removal method and a nitrogen removal apparatus for treating nitrogen-containing wastewater using an anaerobic ammonia oxidation method.
汚水中に含まれる窒素、リンは、湖沼、湾などの閉鎖系水域における富栄養化の原因物質であり、汚水処理工程で効率的に除去されることが望まれる。今日、汚水処理工程から発生する汚泥を処理する方法として、汚泥を嫌気性消化させた後に脱水し、更に乾燥及び焼却などを行って処分する方法がある。これらの処理方法から排出される分離液（脱水分離液）は高濃度の窒素を含んでいる。この分離液が汚水処理系に返流されると、窒素、リン負荷が高くなるために、放流水中の窒素濃度が高くなる原因となるため、高濃度の窒素を含有する廃水を高効率に除去する方法が望まれている。 Nitrogen and phosphorus contained in sewage are substances responsible for eutrophication in closed waters such as lakes and bays, and it is desirable that they be efficiently removed in the sewage treatment process. Today, as a method of treating the sludge generated from the sewage treatment process, there is a method in which the sludge is anaerobically digested and then dewatered, and then dried and incinerated for disposal. The separated liquid (dewatered separated liquid) discharged from these treatment methods contains a high concentration of nitrogen. If this separated liquid is returned to the sewage treatment system, the nitrogen and phosphorus load will be high, which will cause the nitrogen concentration in the effluent water to be high, so waste water containing high concentration of nitrogen will be removed efficiently. How to do that is desired.
汚水から窒素を除去する方法としては生物学的方法が用いられてきている。一般に、汚水中のアンモニア性窒素は、硝化工程と脱窒工程によって窒素ガスまで分解される。具体的には、硝化工程では、アンモニア性窒素は好気条件下で独立栄養性細菌であるアンモニア酸化細菌によって亜硝酸性窒素に酸化され、この亜硝酸性窒素が同じく独立栄養性細菌である亜硝酸酸化細菌によって硝酸まで酸化される。脱窒工程では、従属栄養細菌である脱窒菌が、生成した亜硝酸性窒素および硝酸性窒素を嫌気性条件下で有機物を水素供与体として窒素ガスまで分解する。 Biological methods have been used to remove nitrogen from sewage. In general, ammonia nitrogen in sewage is decomposed to nitrogen gas by nitrification and denitrification steps. Specifically, in the nitrification process, ammonia nitrogen is oxidized to nitrite nitrogen by an autotrophic bacterium ammonia oxidizing bacterium under aerobic conditions, and this nitrite nitrogen is also a nutrient nutrient bacteria. It is oxidized to nitric acid by nitric acid oxidizing bacteria. In the denitrification step, heterotrophic bacteria, denitrifying bacteria, decompose generated nitrite nitrogen and nitrate nitrogen into nitrogen gas as a hydrogen donor under anaerobic conditions.
しかしながら、このような従来の生物学的脱窒法では、アンモニア性窒素を亜硝酸性窒素および硝酸性窒素に酸化するために多量の酸素（空気）を必要とする。更に、脱窒工程では、水素供与体としてのメタノールの使用量が多量であり、ランニングコストを増加させていた。 However, such conventional biological denitrification processes require large amounts of oxygen (air) to oxidize ammonia nitrogen to nitrite nitrogen and nitrate nitrogen. Furthermore, in the denitrification step, the amount of methanol used as a hydrogen donor is large, which increases the running cost.
近年、アンモニア性窒素を水素供与体、亜硝酸性窒素を水素受容体として両者を反応させ、窒素ガスを生成することができる独立栄養性の微生物群を利用した嫌気性アンモニア酸化法の開発が進められている。この反応は以下の（１）式によって進行する。
１．０ＮＨ4 +＋１．３２ＮＯ2 -＋０．０６６ＨＣＯ3 -＋０．１３Ｈ+
→１．０２Ｎ2＋０．２６ＮＯ3 -＋０．０６６ＣＨ2Ｏ0.5Ｎ0.15＋２．０３Ｈ2Ｏ・・・（１）
In recent years, the development of an anaerobic ammonia oxidation method using autotrophic nutrient microbes capable of producing nitrogen gas by reacting ammonia nitrogen with hydrogen donor and nitrite nitrogen as hydrogen acceptor and proceeding It is done. This reaction proceeds according to the following equation (1).
1.0NH 4 + + 1.32NO 2 - + 0.066HCO 3 - + 0.13H +
→ 1.02 N 2 + 0.26 NO 3 − + 0.066 CH 2 O 0.5 N 0.15 + 2.0 3 H 2 O (1)
アンモニアの硝化は、以下の（２）、（３）式に従って進行する。嫌気性アンモニア酸化法では、アンモニアの硝化を亜硝酸化で止めることが肝要であり、硝化処理においてアンモニア性窒素の酸化を亜硝酸性窒素で停止させ、亜硝酸酸化菌の働きにより、硝酸性窒素が生成しないように制御することが必要である。制御方法としては以下の方策がある。
（ａ）亜硝酸化槽内に遊離アンモニアを一定濃度以上残存させ、この遊離アンモニアの毒性を利用して亜硝酸酸化細菌の働きを抑える（アンモニア酸化細菌の活性を亜硝酸酸化細菌の活性よりも高く維持する）。
（ｂ）アンモニアが硝酸まで酸化されないように酸素供給量を制限する。
（ｃ）亜硝酸化槽内に遊離の亜硝酸を一定濃度以上残存させ、この遊離亜硝酸の毒性を利用して亜硝酸酸化細菌の働きを抑える（アンモニア酸化細菌の活性を亜硝酸酸化細菌の活性よりも高く維持する）。
（アンモニア酸化細菌の作用による亜硝酸の生成）
ＮＨ4 +＋３／２Ｏ2→ＮＯ2＋２Ｈ+＋Ｈ2Ｏ ・・・（２）
（亜硝酸酸化細菌の作用による硝酸の生成）
ＮＯ2 -＋１／２Ｏ2→ＮＯ3 - ・・・（３）
The nitrification of ammonia proceeds according to the following equations (2) and (3). In the anaerobic ammonia oxidation method, it is important to stop the nitrification of ammonia with nitrous acid, and in the nitrification process, the oxidation of ammonia nitrogen is stopped with nitrite nitrogen, and the action of nitrite oxidizing bacteria, nitrate nitrogen It is necessary to control so that it does not generate. There are the following measures as a control method.
(A) Remaining free ammonia at a certain concentration or more in the nitrification tank and using the toxicity of this free ammonia to suppress the action of nitrite oxidizing bacteria (the activity of ammonia oxidizing bacteria is greater than the activity of nitrite oxidizing bacteria Keep high).
(B) Limit oxygen supply so that ammonia is not oxidized to nitric acid.
(C) Remaining free nitrite in the nitrite tank at a certain concentration or more, and using the toxicity of the free nitrite to suppress the action of nitrite oxidizing bacteria (ammonia oxidizing bacteria activity of nitrite oxidizing bacteria Keep higher than activity).
(Formation of nitrous acid by the action of ammonia oxidizing bacteria)
NH 4 + + 3 / 2O 2 → NO 2 + 2H + + H 2 O (2)
(Formation of nitric acid by the action of nitrite oxidizing bacteria)
NO 2 - + 1 / 2O 2 → NO 3 - ··· (3)
嫌気性アンモニア酸化法では、窒素収支（１）式から１ｍＭのアンモニアと１．３２ｍＭの亜硝酸とが反応して窒素ガスと０．２６ｍＭの硝酸が発生する。すなわち水中の窒素濃度は３２．４８（＝１×１４＋１．３２×１４）ｍｇ／Ｌから３．６４（＝０．２６×１４）ｍｇＬに低減し、窒素除去率として約８９％を達成できるものの（窒素ガスは溶解度が小さいため水中から放散する）、約１１％の硝酸性窒素が残留することになる。例えば一般的な消化汚泥に含まれるアンモニア性窒素２０００ｍｇ／Ｌの約５７％を亜硝酸性に酸化し、残留する４３％のアンモニアと反応せしめても、１１０ｍｇ／Ｌという高濃度硝酸性窒素が残留する。高率の窒素除去率を達成するためには、さらに残留する硝酸性窒素を除去しなければならない。 In the anaerobic ammonia oxidation method, 1 mM ammonia and 1.32 mM nitrous acid are reacted from nitrogen balance (1) to generate nitrogen gas and 0.26 mM nitric acid. That is, although the nitrogen concentration in water is reduced from 32.48 (= 1 × 14 + 1.32 × 14) mg / L to 3.64 (= 0.26 × 14) mgL, a nitrogen removal rate of about 89% can be achieved. (Nitrogen gas escapes from water due to its low solubility), leaving about 11% of the nitrate nitrogen. For example, even if approximately 57% of 2000 mg / L of ammonia nitrogen contained in general digested sludge is oxidized to nitrite and reacted with the remaining 43% ammonia, highly concentrated nitrate nitrogen of 110 mg / L remains Do. In order to achieve high rates of nitrogen removal, residual nitrate nitrogen must be further removed.
例えば、特開２００６−２７２１７７号公報（特許文献１）では、残留する硝酸性窒素を除去するために、嫌気性アンモニア酸化槽の後段に嫌気性脱窒槽を配備し、メタノール、ＢＯＤ含有廃水、有機酸分離液などの有機炭素源を注入して、独立栄養性脱窒菌を利用して残留硝酸性窒素を還元分解する方法及びシステムを開示している。しかしながら、メタノールのような工業薬品は高価であり処理費用が高額となる。 For example, in Japanese Patent Application Laid-Open No. 2006-272177 (Patent Document 1), in order to remove residual nitrate nitrogen, an anaerobic denitrification tank is disposed downstream of the anaerobic ammonia oxidation tank, and methanol, BOD containing wastewater, organic Disclosed is a method and system for injecting an organic carbon source such as an acid separation liquid to reductively decompose residual nitrate nitrogen using autotrophic denitrifying bacteria. However, industrial chemicals such as methanol are expensive and expensive to process.
アンモニアを含有する有機性廃水を嫌気性アンモニア酸化によって脱窒素し、副生した硝酸も除去する場合は、廃水中の有機物を利用して脱窒素するため、廃水を嫌気性アンモニア酸化工程後段の脱窒工程に分配注入することが特許文献１に開示されている。しかしながら、脱窒工程では、アンモニアは反応せずに脱窒工程からそのまま流出して窒素除去率が低下してしまう。そのため、有機酸分離水についてはアンモニアを分離したのちに脱窒工程に注入することが必要であり、これによりシステム構成が複雑になり、処理操作も煩雑となるという問題がある。 When denitrifying organic wastewater containing ammonia by anaerobic ammonia oxidation and removing nitric acid by-product as well, denitrification is carried out after the anaerobic ammonia oxidation process in order to denitrify using organic substances in the wastewater. It is disclosed by patent document 1 that distribution injection | pouring to a nitridation process is carried out. However, in the denitrification step, ammonia does not react and flows out from the denitrification step as it is, and the nitrogen removal rate is lowered. Therefore, it is necessary to separate ammonia from the organic acid separated water and then inject it into the denitrification step, which causes a problem that the system configuration becomes complicated and the processing operation becomes complicated.
上記課題に鑑み、本発明は、簡単な構成及び操作によって、嫌気性アンモニア酸化槽で処理された流出液中の硝酸をより経済的な方法で除去可能な窒素除去方法及び窒素除去装置を提供する。 In view of the above problems, the present invention provides a nitrogen removal method and a nitrogen removal apparatus capable of removing nitric acid in effluent treated in an anaerobic ammonia oxidation tank by a simple configuration and operation in a more economical method. .
上記課題を解決するために本発明者らが鋭意検討した結果、嫌気性アンモニア酸化処理で処理される流出水を、無酸素工程及び好気性生物処理工程を有する生物処理システムへ導入し、流出液中の硝酸を生物処理システムで脱窒素することが有用であるとの知見を得た。 As a result of intensive studies by the present inventors to solve the above problems, the effluent water treated by anaerobic ammonia oxidation treatment is introduced into a biological treatment system having an anoxic process and an aerobic biological treatment process, and the effluent is treated. We have found that denitrifying nitric acid in biological treatment systems is useful.
以上の知見を基礎として完成した本発明は一側面において、窒素含有廃水を無酸素工程及び好気性生物処理工程を有する生物処理システムで処理する工程と、生物処理システムで発生する有機性汚泥を嫌気性消化工程によりメタンガスに分解する工程と、嫌気性消化工程の流出液中のアンモニアを嫌気性アンモニア酸化工程により窒素ガスに酸化分解する工程と、嫌気性アンモニア酸化工程の流出液を、生物処理システムが備える無酸素工程に導入して流出液中の硝酸を脱窒素する工程とを含む窒素除去方法が提供される。 In one aspect, the present invention completed based on the above findings is a process of treating a nitrogen-containing wastewater with a biological treatment system having an anoxic process and an aerobic biological treatment process, and an anaerobic treatment of organic sludge generated in the biological treatment system. A process of decomposing methane into methane gas by anaerobic digestion process, a process of oxidizing ammonia in the effluent of anaerobic digestion process to nitrogen gas by anaerobic ammonia oxidation process, an effluent of anaerobic ammonia oxidation process, biological treatment system And denitrifying nitric acid in the effluent by introducing it into the anoxic process of
本発明に係る窒素除去方法は一実施態様において、好気性生物処理工程が、アンモニアを硝化する硝化工程を含む。 In one embodiment of the nitrogen removal method according to the present invention, the aerobic biological treatment step includes a nitrification step of nitrifying ammonia.
本発明に係る窒素除去方法は別の一実施態様において、生物処理システムが、窒素含有廃水を、嫌気工程、無酸素工程及び硝化工程で処理する嫌気・無酸素・好気法方式の処理槽を備える。 In another embodiment of the nitrogen removal method according to the present invention, the biological treatment system comprises an anaerobic, anoxic, and aerobic treatment tank in which a nitrogen-containing wastewater is treated in an anaerobic process, an anoxic process, and a nitrification process. Prepare.
本発明は別の一側面において、窒素含有廃水を処理する無酸素槽及び好気性生物処理槽を備える生物処理システムと、生物処理システムで発生する有機性汚泥をメタンガスに分解する嫌気性消化槽と、嫌気性消化槽の流出液中のアンモニアを窒素ガスに酸化分解する嫌気性アンモニア酸化槽と、嫌気性アンモニア酸化槽の流出液を生物処理システムが備える無酸素槽に導入する導入ラインとを備える窒素除去装置が提供される。 In another aspect of the present invention, a biological treatment system comprising an anoxic tank and an aerobic biological treatment tank for treating nitrogen-containing wastewater, and an anaerobic digester that decomposes organic sludge generated in the biological treatment system into methane gas An anaerobic ammonia oxidation tank which oxidizes and decomposes ammonia in the effluent of the anaerobic digester to nitrogen gas, and an introduction line for introducing the effluent of the anaerobic ammonia oxidation tank into an anoxic tank provided in the biological treatment system A nitrogen removal device is provided.
本発明に係る窒素除去装置は一実施態様において、好気性生物処理槽が、アンモニアを硝化する硝化槽を含む。 In one embodiment of the nitrogen removal apparatus according to the present invention, the aerobic biological treatment tank includes a nitrification tank for nitrifying ammonia.
生物処理システムが、窒素含有廃水を、嫌気工程、無酸素工程及び硝化工程で処理する嫌気・無酸素・好気法方式の処理槽を備える。 The biological treatment system comprises an anaerobic, anoxic and aerobic treatment tank for treating nitrogen-containing wastewater in an anaerobic process, an anoxic process and a nitrification process.
本発明によれば、簡単な構成及び操作によって、嫌気性アンモニア酸化槽で処理された流出液中の硝酸をより経済的な方法で除去可能な窒素除去方法及び窒素除去装置が提供できる。 According to the present invention, a simple configuration and operation can provide a nitrogen removal method and a nitrogen removal apparatus capable of removing nitric acid in effluent treated in an anaerobic ammonia oxidation tank in a more economical manner.
以下、図面を参照しながら本発明の実施の形態を説明する。以下に示す実施の形態は、この発明の技術的思想を具体化するための装置や方法を例示するものであってこの発明の技術的思想は構成部品の構造、配置等を下記のものに特定するものではない。 Hereinafter, embodiments of the present invention will be described with reference to the drawings. The embodiment shown below exemplifies an apparatus and a method for embodying the technical idea of the present invention, and the technical idea of the present invention specifies the structure, arrangement and the like of the component parts as follows. It is not something to do.
（第１の実施形態）
本発明の第１の実施の形態に係る窒素除去装置は、図１に示すように、窒素を含有する有機性廃水（以下「窒素含有廃水」という）１を処理する生物処理システム１６と、生物処理システム１６で発生する有機性汚泥（余剰汚泥７）をメタンガスに分解する嫌気性消化槽９と、嫌気性消化槽９の流出液中のアンモニアを窒素ガスに酸化分解する嫌気性アンモニア酸化槽１５と、嫌気性アンモニア酸化槽１５を生物処理システム１６に導入する導入ラインＬ１とを少なくとも備える。
First Embodiment
As shown in FIG. 1, the nitrogen removal apparatus according to the first embodiment of the present invention comprises a biological treatment system 16 for treating nitrogen-containing organic wastewater (hereinafter referred to as "nitrogen containing wastewater") 1, and Anaerobic digestion tank 9, which decomposes organic sludge (surplus sludge 7) generated in the treatment system 16 into methane gas, and anaerobic ammonia oxidation tank 15, which oxidizes ammonia in the effluent of the anaerobic digestion tank 9 to nitrogen gas And at least an introduction line L1 for introducing the anaerobic ammonia oxidation tank 15 into the biological treatment system 16.
生物処理システム１６は、窒素含有廃水１を固形分２−１と分離水２−２とに分離する固液分離槽２と、分離水２−２を実質的に遊離酸素の存在しない嫌気性条件下で処理する無酸素槽３と、無酸素槽３の流出液を好気的に生物処理する好気性生物処理槽４と、好気性生物処理槽４からの流出液を固液分離する固液分離槽５を備えることができる。 The biological treatment system 16 comprises a solid-liquid separation tank 2 for separating the nitrogen-containing wastewater 1 into solid content 2-1 and separated water 2-2, and an anaerobic condition in which the separated water 2-2 is substantially free of free oxygen. Anoxic tank 3 to be treated below, aerobic biological treatment tank 4 to aerobically bioprocess the effluent of anaerobic tank 3 and solid-liquid separation to liquid effluent from aerobic biological treatment tank 4 The separation tank 5 can be provided.
窒素含有廃水１は、固液分離槽２で粗大固形物が固形分２−１と分離水２−２に分離されたのち、分離水２−２が無酸素槽３に導入される。無酸素槽３では、無酸素槽３に流入される分離水２−２中の酸化態窒素（ＮＯX−Ｎ＝ＮＯ2−Ｎ＋ＮＯ3−Ｎ）が、分離水２−２中のＢＯＤ成分によって還元分解される。無酸素槽３の流出液は、好気性生物処理槽４へ導入される。 In the nitrogen-containing wastewater 1, a coarse solid substance is separated into the solid content 2-1 and the separation water 2-2 in the solid-liquid separation tank 2, and then the separation water 2-2 is introduced into the anoxic tank 3. In the anoxic tank 3, the oxidized nitrogen (NO X -N = NO 2 -N + NO 3 -N) in the separated water 2-2 flowing into the anoxic tank 3 is caused by the BOD component in the separated water 2-2 It is reductively decomposed. The effluent of the anoxic tank 3 is introduced into the aerobic biological treatment tank 4.
好気性生物処理槽４は、無酸素槽３からの流出液を好気性生物処理する処理槽であり、例えば流出液を好気性条件下で処理する曝気槽などが利用可能である。曝気槽内では、残留したＢＯＤ物質が酸化分解される。曝気槽の流出液は、固液分離槽５によって分離汚泥と処理水５−１とに分離される。分離汚泥の一部は、返送汚泥６として無酸素槽３に返送され、分離汚泥の残部は余剰汚泥７として、固形分２−１とともに濃縮槽８に導入される。 The aerobic biological treatment tank 4 is a treatment tank that aerobically treats the effluent from the anoxic tank 3, and for example, an aeration tank that treats the effluent under aerobic conditions can be used. In the aeration tank, the remaining BOD substance is oxidatively decomposed. The effluent of the aeration tank is separated into separated sludge and treated water 5-1 by the solid-liquid separation tank 5. A part of the separated sludge is returned to the anoxic tank 3 as the returned sludge 6, and the remaining part of the separated sludge is introduced to the concentration tank 8 together with the solid content 2-1 as the excess sludge 7.
固液分離槽２、５は、沈殿分離、膜分離、ろ過分離、浮上分離などの当業者周知の方法を用いることができる。図示しないが、余剰汚泥７は、固液分離槽２を経由して濃縮槽８に導入してもよい。 The solid-liquid separation tanks 2 and 5 can use methods known to those skilled in the art such as precipitation separation, membrane separation, filtration separation, floatation separation and the like. Although not shown, the excess sludge 7 may be introduced into the concentration tank 8 via the solid-liquid separation tank 2.
濃縮槽８では、窒素含有廃水１から分離された固形分２−１と余剰汚泥７が後段にある嫌気性消化槽９での処理に好適な汚泥濃度に濃縮される。濃縮槽８としては、重力式、遠心式、膜式、浮上式などの当業者周知の装置を用いることができる。濃縮槽８では、固形分２−１と余剰汚泥７とが、濃縮汚泥８−１と濃縮分離水８−２とに分離される。濃縮汚泥８−１は、嫌気性消化槽９へ導入される。濃縮分離水８−２は、固液分離槽２、無酸素槽３又は好気性生物処理槽４に移送される。 In the concentration tank 8, the solid content 2-1 separated from the nitrogen-containing wastewater 1 and the excess sludge 7 are concentrated to a sludge concentration suitable for treatment in the anaerobic digestion tank 9 in the subsequent stage. As the concentration tank 8, devices known to those skilled in the art such as gravity type, centrifugal type, membrane type and floating type can be used. In the concentration tank 8, the solid content 2-1 and the excess sludge 7 are separated into concentrated sludge 8-1 and concentrated separated water 8-2. The concentrated sludge 8-1 is introduced into the anaerobic digestion tank 9. The concentrated separated water 8-2 is transferred to the solid-liquid separation tank 2, the anoxic tank 3 or the aerobic biological treatment tank 4.
嫌気性消化槽９ではメタン発酵が行われ、濃縮汚泥８−１がメタンガス１０にまで分解される。嫌気性消化槽９では浮遊式メタン発酵法が推奨される。発酵工程の撹拌はガス撹拌、インペラを回転する機械撹拌が推奨される。嫌気性消化槽９の流出液１１は固液分離槽１２へ導入され、固液分離槽１２において、流出液１３と未分解残渣１１−１とに分離される。固液分離槽１２では遠心脱水法、沈殿濃縮法など当業者周知の脱水法、濃縮法を用いることができる。 Methane fermentation is performed in the anaerobic digestion tank 9, and the concentrated sludge 8-1 is decomposed to methane gas 10. In the anaerobic digester 9, floating methane fermentation is recommended. For agitation in the fermentation process, gas agitation and mechanical agitation for rotating the impeller are recommended. The effluent 11 of the anaerobic digestion tank 9 is introduced into the solid-liquid separation tank 12 and separated in the solid-liquid separation tank 12 into the effluent 13 and the undegraded residue 11-1. In the solid-liquid separation tank 12, a dehydration method or concentration method known to those skilled in the art such as a centrifugal dehydration method or a precipitation concentration method can be used.
固液分離槽１２の流出液１３に残留するアンモニアは、亜硝酸化槽１４において約５７％のアンモニアが亜硝酸に酸化される。残留する約４３％のアンモニアを含む亜硝酸化槽１４からの流出液は、嫌気性アンモニア酸化槽１５へ導入される。嫌気性アンモニア酸化槽１５では、流出液中のアンモニアが、アンモニア性窒素を電子供与体とし亜硝酸性窒素を電子受容体とする独立栄養性微生物（嫌気性アンモニア酸化細菌）によって、窒素ガスに分解され、一部は硝酸に転換される。 About 57% of the ammonia remaining in the effluent 13 of the solid-liquid separation tank 12 is oxidized to nitrous acid in the nitrite tank 14. The effluent from the nitrification tank 14 containing about 43% of the remaining ammonia is introduced into the anaerobic ammonia oxidation tank 15. In the anaerobic ammonia oxidation tank 15, ammonia in the effluent is decomposed into nitrogen gas by an autotrophic microorganism (anaerobic ammonia oxidizing bacteria) in which ammonia nitrogen is an electron donor and nitrite nitrogen is an electron acceptor. And some are converted to nitric acid.
図示しないが、流出液１３の一部を１００％亜硝酸化し、流出液１３の残部を、亜硝酸化槽１４を経由して嫌気性アンモニア酸化槽１５に導入してもよい。流出液１１のＢＯＤ濃度が高い場合は、嫌気性消化槽９と亜硝酸化槽１４との間に流出液１１中のＢＯＤを酸化させるためのＢＯＤ酸化槽を更に配備してもよい。 Although not shown, a part of the effluent 13 may be converted to 100% nitrite, and the remaining part of the effluent 13 may be introduced into the anaerobic ammonia oxidation tank 15 via the nitrification tank 14. When the BOD concentration of the effluent 11 is high, a BOD oxidation tank for oxidizing the BOD in the effluent 11 may be further provided between the anaerobic digestion tank 9 and the nitrification tank 14.
亜硝酸化槽１４のアンモニア濃度が高濃度の場合には、嫌気性アンモニア酸化槽１５からの流出液１５−１を亜硝酸化槽１４に循環させアンモニア濃度を低減するとｐＨ管理が容易になるが、低減しすぎると亜硝酸で停止せず硝酸にまで酸化する場合がある。 When the ammonia concentration in the nitrification tank 14 is high, if the effluent 15-1 from the anaerobic ammonia oxidation tank 15 is circulated to the nitrification tank 14 to reduce the ammonia concentration, pH control becomes easy. If it is reduced too much, it may not be stopped by nitrous acid but oxidized to nitric acid.
硝酸を含有する該嫌気性アンモニア酸化工程の流出液１５−１は、導入ラインＬ１を介して無酸素槽３に導入され、流出液１５−１中の硝酸が、無酸素槽３中の有機物によって無酸素条件下で窒素ガスに還元分解される。 The effluent 15-1 of the anaerobic ammonia oxidation step containing nitric acid is introduced into the anoxic tank 3 via the introduction line L1, and the nitric acid in the effluent 15-1 is dependent on the organic matter in the anoxic tank 3 It is reductively decomposed to nitrogen gas under anoxic conditions.
図示しないが、流出液１５−１は、固液分離槽２を経由して無酸素槽３に導入してもよい。無酸素槽３の前段に、貯留槽、調整槽等がある場合には、それらの槽を経由して無酸素槽３に流出液１５−１を導入してもよい。 Although not shown, the effluent 15-1 may be introduced into the anoxic tank 3 via the solid-liquid separation tank 2. When a storage tank, an adjustment tank, etc. exist in the front | former stage of the anoxic tank 3, you may introduce the effluent 15-1 into the anoxic tank 3 via those tanks.
無酸素槽３での無酸素工程では、槽を大気と遮断した密閉式が好ましいが、大気開放下でも少量の空気で溶存酸素濃度が検出されない程度の撹拌を行っても、硝酸の除去には同様の効果を得ることができる。固液分離槽２、５、無酸素槽３、好気性生物処理槽４での各処理は、一括していわゆる一般的な生物処理システム１６と呼ばれる。 In the anoxic process in the anoxic tank 3, a closed type in which the tank is shut off from the atmosphere is preferable, but even if stirring is performed to such an extent that the dissolved oxygen concentration is not detected with a small amount of air even under open air, Similar effects can be obtained. The treatments in the solid-liquid separation tank 2, 5, the anoxic tank 3, and the aerobic biological treatment tank 4 are collectively referred to as a so-called general biological treatment system 16.
生物処理システム１６の生物処理方式としては、活性汚泥処理方式のほか、生物膜方式、膜分離活性汚泥方式など当業者に周知の生物処理方式を配備すればよい。膜分離活性汚泥法では、曝気槽の汚泥濃度が高いため、曝気槽（好気性生物処理槽４）から直接、濃縮槽８に導入することも可能である。また、生物処理システム１６として、生物学的脱窒素法として知られる循環式硝化脱窒法、ステップ流入式多段硝化脱窒法、嫌気・無酸素・好気法（Ａ２Ｏ法）など当業者に周知の生物学的脱窒素法を利用することもできる。 As the biological treatment method of the biological treatment system 16, in addition to the activated sludge treatment method, a biological treatment method known to those skilled in the art such as a biofilm method or a membrane separation activated sludge method may be deployed. In the membrane separation activated sludge method, since the sludge concentration of the aeration tank is high, it is also possible to introduce it directly into the concentration tank 8 from the aeration tank (aerobic biological treatment tank 4). In addition, as the biological treatment system 16, organisms known to those skilled in the art such as cyclic nitrification denitrification known as biological denitrification, step inflow multistage nitrification denitrification, and anaerobic / anoxic / aerobic (A2O) are known. Chemical denitrification can also be used.
第１の実施形態に係る窒素除去装置及び窒素除去方法によれば、簡単な構成及び操作によって、嫌気性アンモニア酸化槽で処理された流出液中の硝酸をより経済的な方法で除去できる。 According to the nitrogen removal apparatus and the nitrogen removal method according to the first embodiment, it is possible to remove the nitric acid in the effluent treated in the anaerobic ammonia oxidation tank in a more economical method by the simple configuration and operation.
（第２の実施の形態）
本発明の第２の実施の形態に係る窒素除去装置は、図２に示すように、好気性生物処理槽４が、アンモニアを硝化する硝化槽１７を含み、硝化槽１７の硝化液を無酸素槽３へ循環させる循環ラインＬ２を備える点が、図１に示す窒素除去装置と異なる。
Second Embodiment
In the nitrogen removing apparatus according to the second embodiment of the present invention, as shown in FIG. 2, the aerobic biological treatment tank 4 includes a nitrification tank 17 for nitrifying ammonia, and the nitrification liquid of the nitrification tank 17 is oxygen free. The point which is provided with the circulation line L2 circulated to the tank 3 differs from the nitrogen removing device shown in FIG.
窒素含有廃水１は、固液分離槽２で粗大固形物が固形分２−１と分離水２−２に分離されたのち、分離水２−２が無酸素槽３に導入される。無酸素槽３では、無酸素槽３に流入される分離水２−２中の酸化態窒素（ＮＯX−Ｎ＝ＮＯ2−Ｎ＋ＮＯ3−Ｎ）が、分離水２−２中のＢＯＤ成分によって還元分解される。無酸素槽３の流出液は、好気的条件下にある硝化槽１７へ導入される。 In the nitrogen-containing wastewater 1, a coarse solid substance is separated into the solid content 2-1 and the separation water 2-2 in the solid-liquid separation tank 2, and then the separation water 2-2 is introduced into the anoxic tank 3. In the anoxic tank 3, the oxidized nitrogen (NO X -N = NO 2 -N + NO 3 -N) in the separated water 2-2 flowing into the anoxic tank 3 is caused by the BOD component in the separated water 2-2 It is reductively decomposed. The effluent of the anoxic tank 3 is introduced into the nitrification tank 17 under aerobic conditions.
硝化槽１７では、無酸素槽３からの流出液中のアンモニアが窒素酸化物（ＮＯX）に硝化される。硝化槽１７の流出液の一部は、循環水１８として循環ラインＬ２を介して無酸素槽３に循環される。循環水１８中のＮＯXは無酸素槽３で還元分解される。循環水１８の水量は、循環水１８のアンモニア濃度、目標処理窒素濃度によって適宜選択される。 In the nitrification tank 17, ammonia in the effluent from the anoxic tank 3 is nitrified to nitrogen oxide (NO x ). A part of the effluent from the nitrification tank 17 is circulated as the circulating water 18 to the anoxic tank 3 via the circulation line L2. The NO x in the circulating water 18 is reductively decomposed in the anoxic tank 3. The amount of circulating water 18 is appropriately selected according to the ammonia concentration of circulating water 18 and the target treated nitrogen concentration.
硝化槽１７からの流出液の残部は、固液分離槽５へ導入される。固液分離槽５では、硝化槽１７からの流出液が、分離汚泥と処理水５−１とに分離される。分離汚泥の一部は、返送汚泥６として無酸素槽３に返送され、分離汚泥の残部は余剰汚泥７として、固形分２−１とともに濃縮槽８に導入される。その後は、図１に示す窒素除去装置及び窒素除去方法と実質的に同様である。 The remainder of the effluent from the nitrification tank 17 is introduced into the solid-liquid separation tank 5. In the solid-liquid separation tank 5, the effluent from the nitrification tank 17 is separated into separated sludge and treated water 5-1. A part of the separated sludge is returned to the anoxic tank 3 as the returned sludge 6, and the remaining part of the separated sludge is introduced to the concentration tank 8 together with the solid content 2-1 as the excess sludge 7. The subsequent steps are substantially the same as the nitrogen removal apparatus and the nitrogen removal method shown in FIG.
第２の実施形態に係る窒素除去装置及び窒素除去方法によれば、処理水５−１のアンモニア濃度及び総窒素濃度を更に低減することができる。なお、図示しないが、処理水５−１中の総窒素濃度を更に低減するためには、硝化槽１７と固液分離槽５の間に無酸素槽を別途配備し、固液分離槽５の前段でＮＯXを脱窒素すればよい。また、公知文献（田中ら、「ステップ流入式多段硝化脱窒法に関する調査研究」、２００３年度下水道新技研究所年報、［２／２巻］、ｐ．１４９−１５０）に記載されるようなステップ流入式多段硝化脱窒法の無酸素槽に、嫌気性アンモニア酸化工程の流出液１５−１を導入しても、図２の方式と同様の効果を得ることができる。 According to the nitrogen removal device and the nitrogen removal method of the second embodiment, the ammonia concentration and the total nitrogen concentration of the treated water 5-1 can be further reduced. Although not shown, in order to further reduce the total nitrogen concentration in the treated water 5-1, an anoxic tank is separately provided between the nitrification tank 17 and the solid-liquid separation tank 5, and the solid-liquid separation tank 5 is the NO X at the preceding stage may be denitrification. In addition, a step as described in publicly known documents (Tanaka et al., “Study and research on a step inflow multi-stage nitrification denitrification method, Annual report of the Institute of Sewerage Technology 2003, [2/2], p. 149-150) Even if the effluent 15-1 of the anaerobic ammonia oxidation step is introduced into the anoxic tank of the inflow-type multistage nitrification denitrification method, the same effect as the method of FIG. 2 can be obtained.
（第３の実施の形態）
本発明の第３の実施の形態に係る窒素除去装置は、図３に示すように、生物処理システム１６が、窒素含有廃水１を、嫌気工程（嫌気槽１９）、無酸素工程（無酸素槽３）及び硝化工程（硝化槽１７）で処理する嫌気・無酸素・好気法（Ａ２Ｏ法）方式の処理槽２０を備え、硝化工程の硝化液を無酸素工程へ循環させる循環ラインＬ２を備える点が、図１に示す窒素除去装置と異なる。なお、嫌気工程（嫌気槽１９）、無酸素工程（無酸素槽３）及び硝化工程（硝化槽１７）で処理順序は図３に示す態様に限定されず、装置構成によっては、図３とは異なる順で処理しても構わないことは勿論である。
Third Embodiment
In the nitrogen removal apparatus according to the third embodiment of the present invention, as shown in FIG. 3, the biological treatment system 16 comprises the nitrogen-containing wastewater 1, an anaerobic process (anaerobic tank 19), an anoxic process (anoxic tank) 3) and the treatment tank 20 of the anaerobic, anoxic and aerobic method (A2O method) to be treated in the nitrification step (nitrification tank 17), and comprising the circulation line L2 for circulating the nitrification liquid in the nitrification step to the anoxic step The point is different from the nitrogen removing device shown in FIG. In the anaerobic step (anaerobic tank 19), the anoxic step (anoxic tank 3) and the nitrification step (nitrification tank 17), the treatment order is not limited to the embodiment shown in FIG. Of course, they may be processed in different orders.
窒素含有廃水１は、固液分離槽２で粗大固形物が固形分２−１と分離水２−２に分離されたのち、分離水２−２が、実質的に遊離酸素も結合酸素（ＮＯXをに結合している酸素）の存在しない嫌気槽１９へ導入される。嫌気槽１９には、固液分離槽５からの返送汚泥６中のリン酸が汚泥中から溶出し、嫌気槽１９内のリン濃度が上昇する。嫌気槽１９の流出液は、硝化槽１７からの循環水１８とともに無酸素槽３へ導入される。 In the nitrogen-containing wastewater 1, after the coarse solid substance is separated into the solid content 2-1 and the separated water 2-2 in the solid-liquid separation tank 2, the separated water 2-2 substantially free oxygen also bound oxygen (NO X ) is introduced into the anaerobic tank 19 in the absence of oxygen). In the anaerobic tank 19, the phosphoric acid in the return sludge 6 from the solid-liquid separation tank 5 is eluted from the sludge, and the phosphorus concentration in the anaerobic tank 19 is increased. The effluent from the anaerobic tank 19 is introduced into the anoxic tank 3 together with the circulating water 18 from the nitrification tank 17.
無酸素槽３では、無酸素槽３に流入される嫌気槽１９からの流出液及び循環水１８中の酸化態窒素（ＮＯX−Ｎ＝ＮＯ2−Ｎ＋ＮＯ3−Ｎ）が、嫌気槽１９からの流出液中のＢＯＤ成分によって還元分解される。無酸素槽３からの流出水は、好気的条件下にある硝化槽１７に導入される。硝化槽１７では、無酸素槽３からの流出液中のアンモニアが窒素酸化物（ＮＯX）に硝化され、嫌気槽１９で溶出したリンが活性汚泥に吸収される。 In the anoxic tank 3, the effluent from the anaerobic tank 19 flowing into the anoxic tank 3 and the oxidized nitrogen (NO X −N = NO 2 −N + NO 3 −N) in the circulating water 18 are separated from the anaerobic tank 19. It is reductively degraded by the BOD component in the effluent of Effluent water from the anoxic tank 3 is introduced into the nitrification tank 17 under aerobic conditions. In the nitrification tank 17, ammonia in the effluent from the anoxic tank 3 is nitrified to nitrogen oxides (NO x ), and phosphorus eluted in the anaerobic tank 19 is absorbed by the activated sludge.
硝化槽１７の流出液の一部は、循環水１８として循環ラインＬ２を介して無酸素槽３に循環される。硝化槽１７の流出液の残部は、固液分離槽５において、分離汚泥と処理水５−１とに分離される。その後は、図１に示す窒素除去装置及び窒素除去方法と実質的に同様である。 A part of the effluent from the nitrification tank 17 is circulated as the circulating water 18 to the anoxic tank 3 via the circulation line L2. The remaining part of the effluent of the nitrification tank 17 is separated in the solid-liquid separation tank 5 into separated sludge and treated water 5-1. The subsequent steps are substantially the same as the nitrogen removal apparatus and the nitrogen removal method shown in FIG.
第３の実施の形態に係る窒素除去装置及び窒素除去方法によれば、処理水５−１のアンモニア濃度及び総窒素濃度、更にリン酸濃度を低減することができる。なお、図示しないが、処理水５−１中の総窒素濃度を更に低減するためには、硝化槽１７と固液分離槽５の間に無酸素槽を別途配備し、固液分離槽５の前段でＮＯXを脱窒素すればよい。また、公知文献（安田卓生、「下水処理実施設におけるステップ流入式嫌気好気法における脱窒・脱りんについて」、北海道大学衛生工学シンポジウム論文集、１９９３年１１月１日、１：ｐ．２０５−２０７）に記載されるような、生物学的脱窒脱リン法であるステップ流入式嫌気好気法の無酸素槽に嫌気性アンモニア酸化工程の流出液１５−１を導入しても図３の方式と同様の効果を得ることができる。 According to the nitrogen removal apparatus and the nitrogen removal method of the third embodiment, the ammonia concentration and the total nitrogen concentration of the treated water 5-1, and the phosphoric acid concentration can be further reduced. Although not shown, in order to further reduce the total nitrogen concentration in the treated water 5-1, an anoxic tank is separately provided between the nitrification tank 17 and the solid-liquid separation tank 5, and the solid-liquid separation tank 5 is the NO X at the preceding stage may be denitrification. In addition, well-known literature (Takuo Yasuda, "Denitrification and dephosphorization in the step-flow anaerobic aerobic method in the sewage treatment implementation facility, Proceedings of the Hokkaido University Sanitation Engineering Symposium, November 1, 1993, 1: p. 205 Even if the effluent 15-1 of the anaerobic ammonia oxidation step is introduced into the anoxic tank of step-flow type anaerobic aerobic method which is a biological denitrification and dephosphorization method as described in -207), Fig. 3 The same effect as the method of
嫌気槽１９において活性汚泥に吸収されたリンは、嫌気条件下にある濃縮槽８及びメタン発酵が行われる嫌気性消化槽９で溶出するので、固液分離槽１２でリンを不溶化する無機凝集剤を添加して、分離除去することができる。図示しないが、メタン発酵工程を行う嫌気性消化槽９と亜硝酸化槽１４の間にヒドロキシアパタイト（ＨＡＰ）又はリン酸マグネシウムアンモニウム（ＭＡＰ）精製装置を配備することにより、リンを回収してもよい。 The phosphorus absorbed in the activated sludge in the anaerobic tank 19 is eluted in the concentration tank 8 under anaerobic conditions and the anaerobic digestion tank 9 in which methane fermentation is performed. Therefore, the inorganic coagulant insolubilizing the phosphorus in the solid-liquid separation tank 12 Can be separated and removed. Although not shown, phosphorus may be recovered by providing a hydroxyapatite (HAP) or magnesium ammonium phosphate (MAP) purification apparatus between the anaerobic digestion tank 9 performing the methane fermentation process and the nitrification tank 14. Good.
以下に本発明の実施例を比較例と共に示すが、これらの実施例は本発明及びその利点をよりよく理解するために提供するものであり、発明が限定されることを意図するものではない。 Examples of the present invention are given below together with comparative examples, but these examples are provided to better understand the present invention and its advantages, and are not intended to limit the invention.
（第１実施例）
第１実施例では、図１に示す窒素除去装置の構成に準拠して表１の実験装置を用いて表２の流量（設定値）において有機性廃水の窒素除去処理を実施した。なお、表１の無酸素槽は図１の無酸素槽３、曝気槽は好気性生物処理槽４、沈殿槽は固液分離槽５、濃縮槽は濃縮槽８、回分式遠心脱水機は固液分離槽１２、亜硝酸化槽は亜硝酸化槽１４、嫌気性アンモニア酸化槽は嫌気性アンモニア酸化槽１５に相当する。その結果、表３に示す処理水質（１４日間の平均値サンプル採取日１０日）を得ることができた。表３より嫌気性アンモニア酸化槽流出水中のＮＯ2−Ｎ，ＮＯ3−Ｎは無酸素槽で完全に脱窒素されていることがわかる。
(First embodiment)
In the first example, nitrogen removal treatment of organic wastewater was carried out at the flow rate (set value) of Table 2 using the experimental device of Table 1 in accordance with the configuration of the nitrogen removal device shown in FIG. The anoxic tank in Table 1 is the anoxic tank 3 in Figure 1, the aeration tank is the aerobic biological treatment tank 4, the sedimentation tank is the solid-liquid separation tank 5, the concentration tank is the concentration tank 8, and the batch centrifugal dehydrator is solid. The liquid separation tank 12 and the nitrification tank correspond to the nitrification tank 14, and the anaerobic ammonia oxidation tank corresponds to the anaerobic ammonia oxidation tank 15. As a result, it was possible to obtain the treated water quality shown in Table 3 (average value sampling day 10 days for 14 days). It can be seen from Table 3 that NO 2 -N and NO 3 -N in the anaerobic ammonia oxidation tank effluent water are completely denitrified in the anoxic tank.
（第２実施例）
第２実施例では、図２に示す窒素除去装置の構成に準拠して、好気性生物処理工程としてアンモニアを硝化する消化液循環法を用いた。表４の実験装置を用いて、表５の流量（設定値）において有機性廃水の窒素除去処理を実施したところ、表６に示す処理水質（１４日間の平均値サンプル採取日１０日）を得ることができた。表６より嫌気性アンモニア酸化槽流出水中のＮＯ2−Ｎ，ＮＯ3−Ｎは原水のＢＯＤ成分によって無酸素槽で完全に脱窒素され、なおかつ生物処理工程処理水の総無機性窒素の除去率は（２２−４．１）／２２×１００＝８１％となり、実施例１の総無機性窒素除去率（２２−１３．６）／２２×１００＝３８に比較して高率の除去率が得られた。
Second Embodiment
In the second embodiment, based on the configuration of the nitrogen removal apparatus shown in FIG. 2, a digestive fluid circulation method of nitrifying ammonia was used as an aerobic biological treatment process. When nitrogen removal treatment of organic wastewater is carried out at the flow rate (set value) of Table 5 using the experimental device of Table 4, treated water quality shown in Table 6 (average value sampling day of 10 days of 14 days) is obtained I was able to. From Table 6, NO 2 -N and NO 3 -N in anaerobic ammonia oxidation tank effluent water are completely denitrified in an anoxic tank by BOD component of raw water, and removal rate of total inorganic nitrogen in biological treatment process treated water (22-4.1) / 22 × 100 = 81%, and the removal rate of the high rate is higher than the total inorganic nitrogen removal rate of Example 1 (22-13.6) / 22 × 100 = 38. It was obtained.
（第３実施例）
第３実施例では、図３に示す窒素除去装置の構成に準拠して、生物学的脱リン法である嫌気無酸素好気法を用いた。実施例２の表４の実験装置の無酸素槽の前段に５０Ｌの嫌気槽を配備し、表３の流量条件で約３ヶ月間実施した。その結果、総無機性窒素の除去率は実施例２とほぼ同等であったが、リン除去率は実施例２では（２．８−１．５）／２．８×１００＝４６％であったが、実施例３では８９％を達成できた。
Third Embodiment
In the third embodiment, the anaerobic anoxic aerobic method, which is a biological dephosphorization method, was used according to the configuration of the nitrogen removal apparatus shown in FIG. A 50 L anaerobic tank was disposed upstream of the anoxic tank of the experimental apparatus of Table 4 of Example 2 and carried out for about 3 months under the flow conditions of Table 3. As a result, the removal rate of total inorganic nitrogen was almost the same as in Example 2, but the phosphorus removal rate in Example 2 was (2.8-1.5) /2.8×100=46%. However, in Example 3, 89% could be achieved.
１…窒素含有廃水
２…固液分離槽
３…無酸素槽
４…好気性生物処理槽
５…固液分離槽
６…返送汚泥
７…余剰汚泥
８…濃縮槽
９…嫌気性消化槽
１０…メタンガス
１１…流出液
１２…固液分離槽
１３…流出液
１４…亜硝酸化槽
１５…嫌気性アンモニア酸化槽
１６…生物処理システム
１７…硝化槽
１８…循環水
１９…嫌気槽
２０…処理槽
DESCRIPTION OF SYMBOLS 1 ... nitrogen containing wastewater 2 ... solid-liquid separation tank 3 ... anoxic tank 4 ... aerobic biological treatment tank 5 ... solid-liquid separation tank 6 ... return sludge 7 ... surplus sludge 8 ... concentration tank 9 ... anaerobic digestion tank 10 ... methane gas 11: Effluent 12: Solid-liquid separation tank 13: Effluent 14: Nitrite tank 15: Anaerobic ammonia oxidation tank 16: Biological treatment system 17: Nitrification tank 18: Circulating water 19: Anaerobic tank 20: Treatment tank
Claims (8)
前記生物処理システムで発生する有機性汚泥を嫌気性消化工程によりメタンガスに分解する工程と、
前記嫌気性消化工程の流出液中のアンモニアを、浮遊媒体を用いて亜硝酸化処理する亜硝酸化処理工程及び該亜硝酸化処理工程に続く嫌気性アンモニア酸化工程により窒素ガスに酸化分解する工程と、
前記嫌気性アンモニア酸化工程の流出液を、前記生物処理システムが備える無酸素工程に導入して前記流出液中の硝酸を脱窒素する工程と
を含む窒素除去方法。 Treating the nitrogen containing wastewater with a biological treatment system comprising an anoxic process and an aerobic biological treatment process;
A step of decomposing organic sludge generated in the biological treatment system into methane gas by an anaerobic digestion step;
A process of oxidizing and decomposing ammonia in the effluent of the anaerobic digestion process into nitrogen gas by a nitrification process step of nitrifying treatment using a floating medium and an anaerobic ammonia oxidation step subsequent to the nitrification process step When,
Introducing the effluent of the anaerobic ammonia oxidation step into an anoxic step included in the biological treatment system to denitrify nitric acid in the effluent.
前記無酸素工程及び前記好気性生物処理工程により得られた処理水を更に脱窒素処理する無酸素工程を更に含む請求項１〜３のいずれか１項に記載の窒素除去方法。The nitrogen removal method according to any one of claims 1 to 3, further comprising an anoxic step of denitrifying the treated water obtained by the anoxic step and the aerobic biological treatment step.
前記生物処理システムで発生する有機性汚泥をメタンガスに分解する嫌気性消化槽と、
前記嫌気性消化槽の流出液中のアンモニアを浮遊媒体を用いて亜硝酸化処理する亜硝酸化処理槽と、
前記亜硝酸化処理槽の流出液を窒素ガスに酸化分解する嫌気性アンモニア酸化槽と、
前記嫌気性アンモニア酸化槽の流出液を前記生物処理システムが備える前記無酸素槽に導入する導入ラインと
を備える窒素除去装置。 A biological treatment system comprising an anoxic tank for treating nitrogen-containing wastewater and an aerobic biological treatment tank;
An anaerobic digester that decomposes organic sludge generated by the biological treatment system into methane gas;
A nitrification treatment tank for nitriding the ammonia in the effluent of the anaerobic digestion tank using a floating medium,
An anaerobic ammonia oxidation tank that oxidizes and decomposes the effluent of the nitrification treatment tank to nitrogen gas;
An introduction line for introducing the effluent of the anaerobic ammonia oxidation tank into the anoxic tank of the biological treatment system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015136488A JP6491056B2 (en) | 2015-07-07 | 2015-07-07 | Nitrogen removal method and nitrogen removal apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015136488A JP6491056B2 (en) | 2015-07-07 | 2015-07-07 | Nitrogen removal method and nitrogen removal apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2017018861A JP2017018861A (en) | 2017-01-26 |
| JP6491056B2 true JP6491056B2 (en) | 2019-03-27 |
Family
ID=57887525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2015136488A Active JP6491056B2 (en) | 2015-07-07 | 2015-07-07 | Nitrogen removal method and nitrogen removal apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP6491056B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020220922A1 (en) * | 2019-04-30 | 2020-11-05 | 北京工业大学 | Method and apparatus for treating urban sewage by coupling anaerobic ammonia oxidation with endogenous short-range denitrification of anoxic zone of aoa process |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7507096B2 (en) * | 2018-12-21 | 2024-06-27 | 国立大学法人高知大学 | Wastewater treatment device and wastewater treatment method |
| CN111977797B (en) * | 2020-08-25 | 2022-11-22 | 中生源(海南)生态环境发展有限公司 | Wastewater treatment system and process for synchronous denitrification and dephosphorization of AxOx |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4678577B2 (en) * | 2004-11-05 | 2011-04-27 | 株式会社日立プラントテクノロジー | Wastewater treatment system |
| JP2006305488A (en) * | 2005-04-28 | 2006-11-09 | Kobe Steel Ltd | Method of treating organic sludge |
| JP2010201394A (en) * | 2009-03-05 | 2010-09-16 | Hitachi Plant Technologies Ltd | Nitrous acid type nitrification reaction sludge, method and apparatus for manufacturing the same, and method and apparatus of wastewater treatment |
| JP4995215B2 (en) * | 2009-03-23 | 2012-08-08 | 前澤工業株式会社 | Sewage treatment equipment |
| JP5333954B2 (en) * | 2011-02-02 | 2013-11-06 | 株式会社石垣 | Nitrogen removal system and nitrogen removal method of dehydrated filtrate |
| JP5862082B2 (en) * | 2011-07-08 | 2016-02-16 | 株式会社Ihi | Waste water treatment method and waste water treatment apparatus |
| FR2986226B1 (en) * | 2012-01-27 | 2014-02-14 | Veolia Water Solutions & Tech | METHOD FOR TREATING AN EFFLUENT TO BREAK THE PHOSPHATE CONTENT COMPRISING AN OPTIMIZED WET THERMAL TREATMENT STEP AND CORRESPONDING INSTALLATION |
-
2015
- 2015-07-07 JP JP2015136488A patent/JP6491056B2/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020220922A1 (en) * | 2019-04-30 | 2020-11-05 | 北京工业大学 | Method and apparatus for treating urban sewage by coupling anaerobic ammonia oxidation with endogenous short-range denitrification of anoxic zone of aoa process |
| US11319230B2 (en) | 2019-04-30 | 2022-05-03 | Beijing University Of Technology | Method and apparatus for treating municipal sewage by AOA process via endogenous partial denitrification coupled with anammox in anoxic zone |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2017018861A (en) | 2017-01-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101828212B1 (en) | Wastewater treatment system using anaerobic ammonium oxidation in mainstream | |
| JP5592677B2 (en) | Biological nitrogen treatment method of ammonia containing wastewater | |
| JP2007105631A (en) | Method and device for treating organic waste water | |
| KR102099380B1 (en) | The Method to Remove Nitrogen and Phosphorus from Wastewater by Changing of Reactor and Recycle Method of Conventional Nutrient Removal Process and by Combining Anaerobic Ammonium Oxidation(ANAMMOX) Process | |
| JP4649911B2 (en) | Treatment of organic matter and nitrogen-containing wastewater | |
| JP5186420B2 (en) | Waste water treatment method and waste water treatment equipment | |
| JP5006845B2 (en) | Method for suppressing generation of nitrous oxide | |
| JP6445855B2 (en) | Nitrogen treatment method and nitrogen treatment apparatus | |
| JP2008126143A (en) | Water treatment method | |
| JP2006325512A (en) | Waste water-treating system | |
| JP3925902B2 (en) | Biological nitrogen removal method and apparatus | |
| JP4734996B2 (en) | Biological treatment method and apparatus for nitrogen-containing water | |
| KR20140063454A (en) | Apparatus and method for treatment wastewater | |
| JP4302341B2 (en) | Biological nitrogen removal method and apparatus | |
| KR102144118B1 (en) | Method for Removing Nitrogen and Phosphorus from Wastewater by Nutrient Removal Process via Nitrite and by Combining Anaerobic Ammonium Oxidation(ANAMMOX) Process | |
| JP6491056B2 (en) | Nitrogen removal method and nitrogen removal apparatus | |
| JP2007105630A (en) | Method for treating organic waste water | |
| JP6084150B2 (en) | Denitrification treatment method and denitrification treatment apparatus | |
| KR100838846B1 (en) | Method for treating recycle water of wastewater treatment | |
| WO2013084972A1 (en) | Processing system and processing method for nitrogen-containing organic waste water | |
| JP4570550B2 (en) | Nitrogen removal method and apparatus for high concentration organic wastewater | |
| KR100430382B1 (en) | Treatment method for livestock waste water including highly concentrated organoc, nitrogen and phosphate and treatment system used therein | |
| JP2001079593A (en) | Removing method of nitrogen in waste water | |
| JP2000061494A (en) | Biological treatment of ammonia nitrogen | |
| JP3600220B2 (en) | Wastewater treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20171208 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20181030 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20181031 |
|
| A601 | Written request for extension of time |
Free format text: JAPANESE INTERMEDIATE CODE: A601 Effective date: 20181228 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20190206 |
|
| 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: 20190219 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20190228 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 6491056 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| 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 |