JP4141366B2 - Biological treatment method and apparatus for digested sludge - Google Patents
Biological treatment method and apparatus for digested sludge Download PDFInfo
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- JP4141366B2 JP4141366B2 JP2003350809A JP2003350809A JP4141366B2 JP 4141366 B2 JP4141366 B2 JP 4141366B2 JP 2003350809 A JP2003350809 A JP 2003350809A JP 2003350809 A JP2003350809 A JP 2003350809A JP 4141366 B2 JP4141366 B2 JP 4141366B2
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- 239000010802 sludge Substances 0.000 title claims description 58
- 238000000034 method Methods 0.000 title claims description 16
- 239000007788 liquid Substances 0.000 claims description 37
- 238000000926 separation method Methods 0.000 claims description 30
- 238000012545 processing Methods 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 241000894006 Bacteria Species 0.000 claims description 5
- 230000001546 nitrifying effect Effects 0.000 claims description 5
- 230000029087 digestion Effects 0.000 claims 1
- 239000012530 fluid Substances 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 229920000642 polymer Polymers 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- -1 digested sludge Chemical compound 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000009969 flowable effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Description
本発明は、窒素、ＳＳ含有有機性排液の生物学的処理方法に係り、特に、高濃度のＳＳ及び窒素を含有する消化汚泥の生物学的処理方法と装置に関する。 The present invention relates to a biological treatment method for nitrogen and SS-containing organic effluent, and more particularly to a biological treatment method and apparatus for digested sludge containing high concentrations of SS and nitrogen.
従来、消化汚泥中のＳＳ及び窒素を生物学的に処理する方法としては、図２に示すように、固液分離、脱窒槽、硝化槽、沈殿池の順番に処理施設を配置し、消化汚泥中のＳＳ分を固液分離して取り除いたのち、脱離液のみを脱窒槽に導き、この脱窒槽に沈殿池において濃縮・分離した活性汚泥を返送すると共に、硝化槽から流出した硝化液を循環し、ＳＳの除去及び脱窒を行う方法が挙げられる。しかし、近年、初期コスト及び運転コストの低減が強く求められており、消化汚泥のような高濃度のＳＳ及び窒素を含有する有機性排液を低コストで高効率に処理するフローについて検討する必要がある。
本発明者らは、消化汚泥を低コストで処理できる可能性を有するフローとして、消化汚泥を直接、脱窒槽に導く処理フローについて検討した。しかし、上記処理フローを検討していく上で、次の問題に遭遇した。消化汚泥を直接投入した場合、消化汚泥のＳＳ濃度が６，０００〜１０，０００ｍｇ／Ｌ、Ｔ−Ｎが３，０００〜６，０００ｍｇ／Ｌと高いため、硝化槽にかかる窒素容積負荷が大きくなってしまい、十分な平均汚泥滞留時間（Ａ−ＳＲＴ）を確保できず、硝化が良好に進行しない。Ａ−ＳＲＴを確保するためには、（１）反応時間を長くするかあるいは槽容積を大きくする、（２）硝化槽及び脱窒槽のＭＬＳＳを高くする、の２つの解決法が考えられる。しかし、（１）の解決法では処理装置が大きくなり、（２）の解決法では硝化槽内のＭＬＳＳを高く維持できるほど、十分に濃縮・分離ができないため、濃縮に初期コスト及び運転コストの高い膜分離装置を使用することになる。そこで、本発明では、低コストで高濃度のＳＳ及び窒素を含有する消化汚泥を処理できる生物学的処理方法と装置を提供することを課題とする。 The present inventors examined a processing flow for directly guiding the digested sludge to the denitrification tank as a flow having a possibility of processing the digested sludge at a low cost. However, the following problems were encountered in examining the above processing flow. When digested sludge is added directly, the SS concentration of digested sludge is as high as 6,000 to 10,000 mg / L and TN is as high as 3,000 to 6,000 mg / L. As a result, sufficient average sludge residence time (A-SRT) cannot be secured, and nitrification does not proceed well. In order to secure A-SRT, there are two possible solutions: (1) increasing the reaction time or increasing the tank volume, and (2) increasing the MLSS of the nitrification tank and denitrification tank. However, in the solution of (1), the processing apparatus is large, and in the solution of (2), the concentration and separation cannot be sufficiently performed so that the MLSS in the nitrification tank can be maintained high. A high membrane separator will be used. Therefore, an object of the present invention is to provide a biological treatment method and apparatus capable of treating digested sludge containing high concentrations of SS and nitrogen at low cost.
上記の課題を解決するために、本発明では、消化汚泥を生物学的に処理する方法において、前記消化汚泥を固液分離することなく直接脱窒槽に流入して処理し、該処理した脱窒槽の流出液は、硝化菌を保持させるための流動できる担体を投入した硝化槽で処理し、該処理液から担体を分離後の硝化液の一部は、前記脱窒槽に循環すると共に、該硝化液の残部は汚泥処理工程を兼ねた濃縮分離をして、分離液を処理水とし、濃縮汚泥を余剰汚泥として排出することを特徴とする消化汚泥の生物学的処理方法としたものである。
前記処理方法において、消化汚泥は、ＳＳ濃度が６，０００〜１２，０００ｍｇ／Ｌを用いることができる。
また、本発明では、消化汚泥を生物学的に処理する装置において、該消化汚泥を固液分離することなく直接処理する脱窒槽と、該脱窒槽の流出液を処理する硝化菌を保持させる流動担体を投入した硝化槽と、該硝化槽に備えた担体分離手段と、該担体を分離した硝化液の一部を前記脱窒槽に循環する循環流路と、該硝化液の残部を汚泥処理工程を兼ねて濃縮分離する濃縮分離装置とを有することを特徴とする消化汚泥の生物学的処理装置としたものである。
前記処理装置において、濃縮分離装置は機械濃縮装置を用いるのがよい。
In order to solve the above-mentioned problems, in the present invention, in the method of biologically treating digested sludge , the digested sludge is treated by directly flowing into the denitrification tank without solid-liquid separation, and the treated denitrification tank The effluent is treated in a nitrification tank charged with a flowable carrier for holding nitrifying bacteria, and a part of the nitrification liquid after separating the carrier from the treatment liquid is circulated to the denitrification tank and the nitrification the remainder of the liquid is concentrated separation also serves as a sludge treatment process, the separation liquid and the treated water, in which the concentrated sludge was biological treatment method digested sludge, characterized in that the discharged as excess sludge.
In the said processing method , SS density | concentration can use 6,000-12,000 mg / L for digested sludge .
In the present invention, an apparatus for processing a digested sludge biologically, to hold a denitrification tank for processing directly without solid-liquid separation of the digested sludge, the nitrifying bacteria for processing effluent denitrification tank flow A nitrification tank charged with a carrier, a carrier separation means provided in the nitrification tank, a circulation channel for circulating a part of the nitrification liquid from which the carrier has been separated to the denitrification tank, and a sludge treatment step for the remainder of the nitrification liquid A biological treatment apparatus for digested sludge , characterized in that it has a concentration and separation device that also performs concentration separation.
In the processing apparatus, it is preferable to use a mechanical concentrator as the concentrator / separator.
本発明によれば、消化汚泥のような高濃度のＳＳ及び窒素を含有する有機性排液を固液分離することなく、省スペースで高効率な生物処理が可能となる。また、消化汚泥のような高濃度のＳＳ及び窒素を含有する有機性排液を固液分離することなく、直接脱窒槽に流入させることから、汚泥発生量を低減でき、ポリマー等の薬品使用量を抑えることができるため、低コスト化が実現できる。また、余剰汚泥の濃縮操作を、活性汚泥混合液の固液分離操作をもって行うことができるため、濃縮操作を省くことができ、低コスト化が実現できる。本発明は、現在の消化汚泥の処理フローにとってかわる新たな処理方法となるものと確信する。 According to the present invention, space-saving and highly efficient biological treatment is possible without solid-liquid separation of organic drainage containing high concentrations of SS and nitrogen such as digested sludge. In addition, organic wastewater containing high concentrations of SS and nitrogen, such as digested sludge, is directly flowed into the denitrification tank without solid-liquid separation, reducing the amount of sludge generated and using chemicals such as polymers. Therefore, the cost can be reduced. Moreover, since the concentration operation of excess sludge can be performed by the solid-liquid separation operation of the activated sludge mixed liquid, the concentration operation can be omitted and the cost can be reduced. It is certain that the present invention will be a new treatment method that replaces the current treatment flow of digested sludge.
次に、本発明の構成を詳細に説明する。本発明で提案する処理フローは、図１に示すように、脱窒槽、硝化槽、固液分離の順番に処理施設を配置する。消化汚泥は固液分離することなく、直接脱窒槽に流入させ、脱窒槽の流出液は硝化菌を保持させるための担体を投入した硝化槽で処理する。すなわち、従来法では、消化汚泥を固液分離した後、生物処理を行っていたが、本発明では、消化汚泥を固液分離することなく、直接脱窒槽に流入させて生物処理を行うことから、生物処理工程において消化汚泥中のＳＳの一部が分解され、汚泥発生量を低減でき、ポリマー等の薬品使用量を抑えることができるため、低コスト化が実現できる。また、本発明によれば、１２，０００ｍｇ／Ｌ程度の高濃度ＭＬＳＳにおいても、担体による硝化性能の向上が見られるため、消化汚泥を直接処理しても硝化槽の容積をコンパクトにできる。 Next, the configuration of the present invention will be described in detail. In the processing flow proposed in the present invention, processing facilities are arranged in the order of denitrification tank, nitrification tank, and solid-liquid separation, as shown in FIG. Digested sludge flows directly into the denitrification tank without solid-liquid separation, and the effluent from the denitrification tank is treated in a nitrification tank containing a carrier for holding nitrifying bacteria. That is, in the conventional method, the biological treatment is performed after solid-liquid separation of the digested sludge, but in the present invention, the biological treatment is performed by directly flowing into the denitrification tank without performing solid-liquid separation of the digested sludge. In the biological treatment process, part of the SS in the digested sludge is decomposed, the amount of sludge generated can be reduced, and the amount of chemicals such as polymers can be suppressed, so that the cost can be reduced. Further, according to the present invention, even at a high concentration MLSS of about 12,000 mg / L, the nitrification performance is improved by the carrier, so that the volume of the nitrification tank can be made compact even if the digested sludge is directly processed.
担体分離後の硝化液の一部は、目標の処理水窒素濃度に応じた量を脱窒槽に循環すると共に、残りは処理水と余剰汚泥に固液分離する。固液分離には、膜分離装置なども使用できるが、遠心濃縮機などの機械濃縮装置を用いることで、汚泥処理工程の濃縮操作を兼ねることができる。すなわち、従来法では、余剰汚泥は濃縮した後、脱水処理を行っていたのに対し、本発明では、濃縮操作を活性汚泥混合液の固液分離操作で行うことができるため、濃縮操作の工程を省くことができ、低コスト化が実現できる。また、生物処理槽の活性汚泥濃度（ＭＬＳＳ）を高めたい場合には、濃縮汚泥の一部を脱窒槽に返送してもよい。分離液は、下水放流などの場合には、直接処理水として放流可能であるが、より清澄な処理水が要求される場合には、必要に応じて凝集処理やろ過処理装置などを追加すればよい。 A part of the nitrification liquid after the carrier separation is circulated in the denitrification tank in an amount corresponding to the target treated water nitrogen concentration, and the rest is solid-liquid separated into treated water and excess sludge. For solid-liquid separation, a membrane separation device or the like can be used, but by using a mechanical concentration device such as a centrifugal concentrator, it can also serve as a concentration operation in a sludge treatment process. That is, in the conventional method, excess sludge is concentrated and then dehydrated, whereas in the present invention, the concentration operation can be performed by a solid-liquid separation operation of the activated sludge mixed solution. The cost can be reduced. Moreover, when it is desired to increase the activated sludge concentration (MLSS) of the biological treatment tank, a part of the concentrated sludge may be returned to the denitrification tank. In the case of sewage discharge, the separation liquid can be discharged directly as treated water, but if more clarified treated water is required, a coagulation treatment or filtration treatment device can be added if necessary. Good.
なお、本発明で硝化槽に入れる担体は、粒径１〜１５ｍｍ程度の粒状の親水性ゲル、プラスチック片、スポンジ、発泡性セラミック、高分子担体などが使用でき、担体が安定して流動できる粒径及び担体の材質であればよいが、高濃度のＭＬＳＳでの流動状態を考えると、スポンジが好ましい。また、担体の充填率は、硝化槽の構造、曝気風量、担体の形状ならびに性状に応じて変動するが、担体の流動性を考慮して３０％以下であることが好ましい。
脱窒槽には、担体を入れなくてもかまわないが、微生物固定化担体を入れた方が脱窒速度の上昇が期待できるため、すみやかに硝化脱窒を行う場合には入れた方が好ましい。
The carrier to be put in the nitrification tank in the present invention can be a granular hydrophilic gel, plastic piece, sponge, foamable ceramic, polymer carrier, etc. having a particle size of about 1 to 15 mm, and the carrier can flow stably. Any material may be used as long as it has a diameter and a carrier material, but a sponge is preferable in consideration of a flow state in a high concentration MLSS. Further, the filling rate of the carrier varies depending on the structure of the nitrification tank, the amount of aeration, the shape and properties of the carrier, but is preferably 30% or less in consideration of the fluidity of the carrier.
The denitrification tank does not need to contain a carrier. However, since it is expected that the denitrification rate is increased when the microorganism-immobilized carrier is added, it is preferable to add the carrier when the nitrification denitrification is performed immediately.
以下に、本発明を実施例で具体的に説明する。
実施例１
（ａ）原液
生ごみメタン発酵により発生した消化汚泥（Ｒｗ）；Ｓ−ＢＯＤ：１１，０００ｍｇ／Ｌ、ＳＳ：８，２００ｍｇ／Ｌ、ＮＨ４−Ｎ：４，１００ｍｇ／Ｌ、
水量；０．３ｍ３／ｄ、
（ｂ）循環式硝化脱窒槽
硝化槽；有効容量：１．０ｍ３、水理学的滞留時間（ＨＲＴ）：３．３ｄａｙ、
脱窒槽；有効容量：０．５ｍ３、ＨＲＴ：１．６７ｄａｙ、
設定循環比；４０Ｑ、
（ｃ）微生物固定化担体
形状；１ｃｍ角スポンジ状、
投入量；嵩体積として０．２ｍ３（充填率２０ｖ／ｖ％）、
Hereinafter, the present invention will be specifically described by way of examples.
Example 1
(A) Stock solution Digested sludge generated by garbage methane fermentation (Rw); S-BOD: 11,000 mg / L, SS: 8,200 mg / L, NH 4 -N: 4,100 mg / L,
Water amount: 0.3 m 3 / d,
(B) Circulating nitrification denitrification tank nitrification tank; effective capacity: 1.0 m 3 , hydraulic residence time (HRT): 3.3 day,
Denitrification tank; effective capacity: 0.5 m 3 , HRT: 1.67 day,
Set circulation ratio; 40Q,
(C) Microbe-immobilized carrier shape: 1 cm square sponge shape,
Input amount: 0.2 m 3 as a bulk volume (filling rate 20 v / v%),
（ｄ）運転結果
表１に運転終了後の硝化槽及び脱窒槽の最終水質（Ｔｗ）を示す。硝化槽のろ液のＮＨ４−Ｎは１３ｍｇ／Ｌ、ＮＯｘ−Ｎは４７ｍｇ／Ｌ、Ｔ−Ｎは７６ｍｇ／Ｌ、Ｓ−ＢＯＤは１６ｍｇ／Ｌとなり、きわめて良好に消化汚泥の硝化脱窒が進行した。
比較例１
以下に比較例として従来法を示す。
本発明と同等の処理水質を得るためには、前処理として固液分離を行い、かつ、硝化槽７ｄａｙ、脱窒槽３ｄａｙと処理時間を長くする必要がある。また、後処理として汚泥を濃縮し、一部を返送し、残りを余剰汚泥として処理する必要がある。
（ａ）原液
生ごみメタン発酵により発生した消化汚泥を固液分離した脱離液（Ｒｗ’）；Ｓ−ＢＯＤ：５，０００ｍｇ／Ｌ、Ｔ−Ｎ：２，５００ｍｇ／Ｌ、ＳＳ：３００ｍｇ／Ｌ、
水量：０．３ｍ３／ｄ
（ｂ）循環式硝化脱窒槽
硝化槽；有効容量：１．０ｍ３、Ａ−ＳＲＴ ７ｄａｙ
脱窒槽；有効容量：０．５ｍ３、Ａ−ＳＲＴ ３ｄａｙ
設定循環比；２５Ｑ、ＭＬＳＳ＝４０００ｍｇ／Ｌ
Comparative Example 1
The conventional method is shown below as a comparative example.
In order to obtain a treated water quality equivalent to that of the present invention, it is necessary to perform solid-liquid separation as a pretreatment and to increase the treatment time of the nitrification tank 7 day and the denitrification tank 3 day. Moreover, it is necessary to concentrate sludge as post-processing, to return a part, and to process the remainder as surplus sludge.
(A) Stock solution Desorbed liquid (Rw ′) obtained by solid-liquid separation of digested sludge generated by garbage methane fermentation; S-BOD: 5,000 mg / L, TN: 2,500 mg / L, SS: 300 mg / L,
Water volume: 0.3 m 3 / d
(B) Circulating nitrification denitrification tank nitrification tank; Effective capacity: 1.0 m 3 , A-SRT 7 day
Denitrification tank; effective capacity: 0.5 m 3 , A-SRT 3 day
Set circulation ratio: 25Q, MLSS = 4000mg / L
（ｃ）運転結果
表２に運転終了後の硝化槽及び脱窒槽の最終水質（Ｔｗ’）を示す。
Ｔ−Ｎは８５ｍｇ／Ｌ、Ｓ−ＢＯＤは１０ｍｇ／Ｌとなった。
TN was 85 mg / L and S-BOD was 10 mg / L.
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| JP2003350809A JP4141366B2 (en) | 2003-10-09 | 2003-10-09 | Biological treatment method and apparatus for digested sludge |
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