JP6121165B2 - Anaerobic treatment method and apparatus - Google Patents
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
-
- 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
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Hydrology & Water Resources (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Description
本発明は、汚泥の嫌気性処理方法および装置に関するものである。 The present invention relates to an anaerobic treatment method and apparatus for sludge.
汚泥の嫌気性消化処理は、好気性処理に比べて汚泥発生量が少なく、病原微生物や寄生虫卵も速やかに死滅して安定化し、酸素の供給が不要なので動力消費量も少なく、メタンガスを主成分とするバイオガスも得られることから、省エネルギー的処理方法として古くから適用されている技術である。一方、嫌気性消化槽設備は大容量を必要とし、消化汚泥の処理では薬品費用が高く、かつ、汚泥が難脱水性で脱水汚泥含水率も下げにくいことから、課題点の多い技術でもある。 The anaerobic digestion treatment of sludge produces less sludge than aerobic treatment, promptly kills and stabilizes pathogenic microorganisms and parasite eggs, reduces oxygen consumption, and consumes less power. Since biogas as a component can also be obtained, this technology has been applied for a long time as an energy-saving treatment method. On the other hand, the anaerobic digester equipment requires a large capacity, and the treatment of digested sludge has a high chemical cost, and the sludge is difficult to dehydrate and the water content of the dehydrated sludge is difficult to lower.
したがって、現状の汚泥処分方法としては、汚泥を嫌気性消化することなく、脱水して埋立てたり、脱水して焼却処分する事例がまだまだ多い。例えば、従来の汚泥の嫌気性処理として、図６に示すブロックフロー図で示されるものが挙げられる。このフローについて説明する。 Therefore, as the current sludge disposal methods, there are still many cases in which sludge is dehydrated and landfilled or dehydrated and incinerated without anaerobic digestion. For example, the conventional sludge anaerobic treatment includes the one shown in the block flow diagram of FIG. This flow will be described.
汚泥１は、貯留装置２に送られ、次いで汚泥１は、固液分離装置６に送られ、汚泥濃縮物７と分離液８とに固液分離され、汚泥濃縮物７は、嫌気性消化装置９に送られ、汚泥の嫌気性消化によりバイオガス１０及び嫌気性消化汚泥１１が生成され、バイオガス１０は、バイオガスタンク１０１に送られ、次いでバイオガス１０は、ガス利用設備１０２（例えば、ガスタービン、バイオガスボイラ、ガス燈、乾燥機熱源等）、あるいは余剰ガス燃焼装置１０３に送られる。嫌気性消化汚泥１１は、消化汚泥凝集物調製装置１２に送られ、分離液１４を分離するとともに消化汚泥凝集物１５が調製され、消化汚泥凝集物１５は、脱水装置１６に送られ、分離液１７を分離するとともに脱水ケーキ１８が調製される。分離液８、分離液１４、及び分離液１７は、廃水処理設備１０４等に送られる。消化汚泥凝集物調製装置１２では、凝集剤が添加されることが多い。
The sludge 1 is sent to the
一方、特許文献１には、（ａ）汚泥の混在するし尿を固液分離する前処理工程と、（ｂ）処理工程で分離した固形物を脱水せずに直接嫌気性消化する嫌気性消化工程と、（ｃ）動植物残さ及び固形物を含有する厨芥を嫌気性消化する嫌気性消化工程と、（ｄ）嫌気性消化工程流出液を固形物と分離水に脱水分離する脱水工程、（ｅ）前処理工程の分離水、脱水工程からの分離水を生物学的に酸化、脱窒素する生物処理工程とからなる処理方法により、有機性廃水処理施設の汚泥、浄化槽汚泥等の汚泥、し尿、動植物残さを含有する厨芥を省エネルギー的に処理するとともに、し尿、浄化槽汚泥中の非衛生な篩渣を衛生的にコンポスト化又は固形燃料化する、し尿、厨芥、汚泥の処理方法を提案している。 On the other hand, Patent Document 1 includes (a) a pretreatment process for solid-liquid separation of sludge mixed with human waste, and (b) an anaerobic digestion process for directly anaerobically digesting the solid matter separated in the treatment process without dehydration. And (c) an anaerobic digestion step for anaerobically digesting the plant and animal residue and the solids containing solid matter, (d) a dehydration step for dehydrating and separating the anaerobic digestion step effluent into solids and separated water, (e) Sludge from organic wastewater treatment facilities, sludge such as septic tank sludge, human waste, animals and plants by a treatment method consisting of biological treatment process that biologically oxidizes and denitrifies the separated water from the pretreatment process and the dewatering process It proposes a treatment method for human waste, waste, and sludge that treats waste containing residue in an energy-saving manner, and sanitizes non-hygienic sieve residue in human waste and septic tank sludge.
特許文献２には、廃水処理設備における最初沈殿池から発生する初沈汚泥と最終沈殿池から発生する余剰汚泥とを混合して貯留し、この混合汚泥に凝集剤を添加して１次凝集処理を行い、次に１次凝集処理を終えた混合汚泥をその汚泥濃度が６〜８％となるように濃縮処理し、次いで濃縮処理後の混合汚泥に凝集剤を添加して２次凝集処理を行い、さらに２次凝集処理を行った混合汚泥に脱水処理を施す処理方法により、廃水処理により発生する初沈汚泥と余剰汚泥の２種の汚泥を、１系統で濃縮処理するとともに、後続の脱水工程にとって最適な汚泥濃度まで濃縮、維持することにより、これら廃水汚泥の濃縮、脱水プロセスにおけるトータルの効率を最大限に発揮させる汚泥処理方法及びそのシステムを提案している。
In
また、特許文献３には、固液分離装置の搬送能力を上げるとともに、押圧圧搾効果を増大させるスリット型濃縮機が提案されている。
Further,
廃水処理設備等で発生する汚泥の嫌気性消化処理では、通常はＨＲＴ（水理学的滞留時間：Hydraulic retention time）２０〜３０日とするので大容量の嫌気性消化槽を必要とすることが最大の問題であった。例えば、汚泥ＴＳ（Total Solids）濃度３wt％、処理量１００ｍ３／日の汚泥処理では、通常２０００〜３０００ｍ３もの大型の嫌気性消化槽を設ける必要がある。また、消化汚泥処理では、汚泥凝集や脱水処理に要する薬品費用が高くなり、かつ、汚泥が難脱水性になっていて汚泥含水率も下がりにくいことが問題であった。これは、汚泥の嫌気性消化ではタンパク質が分解されることでアンモニア態窒素が生成され、Ｍアルカリ度（ｐＨ４．８までの酸消費量）も３，０００ｍｇＣａＣＯ３／Ｌ程度以上と高くなり、汚泥凝集の最適ｐＨ条件とされる弱酸性領域から外れていくためである。さらには、汚泥消化によって汚泥中の粗浮遊物（繊維分）も一緒に分解される為、汚泥脱水時の水抜けに大きく寄与する粗浮遊物含率が低下してしまって、脱水ケーキ含水率は高くなってしまう問題もあった。更に、嫌気性消化槽や配管等にリンやカルシウム等の析出物が発生するという問題もある。また、排水中に含まれるケイ素は、通常、シャンプー、リンス、化粧品等に含まれるシリコンオイル等のケイ素化合物に起因するシロキサンの形態である。シロキサンとは、主骨格がＳｉ−Ｏ−で側鎖に炭化水素基を有するケイ素−酸素結合を有する有機化合物を意味する。シロキサンとしては、例えば、ケイ素原子が２〜６で、炭化水素基がメチル基等である線状又は環状のものが挙げられる。シロキサンは水への溶解度が低いことから、下水汚泥を嫌気性消化した場合にはバイオガス中に分配移行するため、バイオガスを発電利用するとガスエンジンなどの発電設備や周辺機器にスケールとなって析出し、発電効率低下や設備メンテナンスに悪影響を及ぼす事例が多く知られ、この防止対策が重要となっている。In anaerobic digestion treatment of sludge generated in wastewater treatment facilities, etc., it is usually HRT (Hydraulic retention time) 20-30 days, so it is most necessary to have a large capacity anaerobic digester It was a problem. For example, sludge TS (Total Solids)
本発明は、上述の点に鑑みてなされたもので、嫌気性消化装置を小型化するとともにリン、カルシウム、シロキサン（シロキサン結合を有するケイ素化合物）等を含む析出物の発生を低減し、廃水処理設備等で発生する汚泥を安定的かつ効率的に嫌気性消化すると共に、バイオガス（特にメタンガス）を効率良く回収することができ、かつ消化汚泥を効率的に脱水することのできる低コスト化が図れる嫌気性処理方法および装置を提供することにある。 The present invention has been made in view of the above-mentioned points, and reduces the generation of precipitates including phosphorus, calcium, siloxane (a silicon compound having a siloxane bond), etc. while reducing the size of an anaerobic digester, and thereby treating wastewater. Cost reduction that enables anaerobic digestion of sludge generated in facilities, etc., as well as efficient recovery of biogas (especially methane gas) and efficient dehydration of digested sludge An object is to provide an anaerobic treatment method and apparatus.
本発明によれば、以下の嫌気性処理方法及び嫌気性処理装置が提供される。
１）汚泥に凝集剤を添加して調製した凝集汚泥を、汚泥濃度４〜１２wt％の汚泥濃縮物と分離液とに固液分離する前処理工程、該汚泥濃縮物を嫌気性消化するとともにバイオガスを回収する嫌気性消化工程、該嫌気性消化工程で調製された嫌気性消化汚泥に、凝集剤と、前記分離液及び水の少なくとも何れかと、を混合して消化汚泥凝集物を調製する工程、及び該消化汚泥凝集物を固液分離して得られる消化汚泥濃縮物を脱水する工程を含む、嫌気性処理方法。
２）汚泥に凝集剤を添加して凝集汚泥を調製する凝集槽、該凝集汚泥を汚泥濃度４〜１２wt％の汚泥濃縮物と分離液とに固液分離して汚泥濃縮物を調製する前処理汚泥濃縮装置、該汚泥濃縮物を嫌気性消化するとともにバイオガスを回収する嫌気性消化装置、該嫌気性消化装置で調製された嫌気性消化汚泥に、凝集剤と、前記分離液及び水の少なくとも何れかと、を混合して消化汚泥凝集物を調製する消化汚泥凝集装置、及び該消化汚泥凝集物を固液分離して得られる消化汚泥濃縮物を脱水する脱水装置を含む、嫌気性処理装置。According to the present invention, the following anaerobic processing methods and anaerobic processing apparatuses are provided.
1) A pretreatment step for solid-liquid separation of agglomerated sludge prepared by adding a flocculant to sludge into a sludge concentrate and a separated liquid having a sludge concentration of 4 to 12 wt%, and biotreating the sludge concentrate anaerobically Anaerobic digestion step for collecting gas, anaerobic digestion sludge prepared in the anaerobic digestion step, a step of preparing a digested sludge aggregate by mixing a flocculant and at least one of the separation liquid and water. And an anaerobic treatment method comprising a step of dehydrating a digested sludge concentrate obtained by solid-liquid separation of the digested sludge aggregate.
2) A coagulation tank for preparing coagulated sludge by adding a coagulant to the sludge, and pretreatment for preparing the sludge concentrate by solid-liquid separation of the coagulated sludge into a sludge concentrate having a sludge concentration of 4 to 12 wt% and a separated liquid. Sludge concentrator, anaerobic digester for anaerobically digesting the sludge concentrate and collecting biogas, anaerobic digested sludge prepared by the anaerobic digester, a flocculant, at least the separation liquid and water An anaerobic treatment apparatus comprising: a digested sludge agglomeration apparatus that mixes any of these to prepare a digested sludge aggregate; and a dehydrator that dehydrates the digested sludge concentrate obtained by solid-liquid separation of the digested sludge aggregate.
本発明の処理方法において、前処理工程で固液分離されて調製される汚泥濃縮物は、４〜１２wt%と従来方法よりも１．５〜２倍以上高濃度の汚泥を含む。この汚泥濃縮物を嫌気性消化処理するため、本発明における嫌気性消化汚泥は、従来方法における嫌気性消化汚泥よりも高いＭアルカリ度及びアンモニア濃度を有する。そのために、嫌気性消化汚泥にそのまま凝集剤を添加して脱水可能なフロックを得ようとすると、多量の凝集剤が必要となる。そこで本発明では、脱水可能な消化汚泥凝集物を得るために、前処理工程で得られた分離液又は水の少なくとも何れかを嫌気性消化汚泥に混合して嫌気性消化汚泥を希釈し、嫌気性消化汚泥と添加される凝集剤との汚泥凝集反応による消化汚泥凝集物の生成をスムーズに行い、凝集剤注入量の低減を図る。また、本発明の前処理工程では、凝集剤を添加して調製した凝集汚泥を汚泥濃縮物と分離液とに分離するため、分離液にはリン等の水溶性乃至親水性の有用資源が含有されることになり、効率的に有用資源を回収することができる。さらに、有用資源を回収することができる前処理工程は、嫌気性消化工程の前に行われるため、嫌気性消化工程に送られる汚泥濃縮物中のリン、シロキサン等は低減され、且つ、汚泥濃度が高濃度であるため、嫌気性消化槽でのリン、シロキサン等を含む析出物の発生を低減することができる。 In the treatment method of the present invention, the sludge concentrate prepared by solid-liquid separation in the pretreatment step contains 4 to 12 wt% of sludge having a concentration 1.5 to 2 times higher than that of the conventional method. In order to anaerobically digest this sludge concentrate, the anaerobic digested sludge in the present invention has higher M alkalinity and ammonia concentration than the anaerobic digested sludge in the conventional method. Therefore, if a flocculant is added to anaerobic digested sludge as it is to obtain a dewaterable floc, a large amount of flocculant is required. Therefore, in the present invention, in order to obtain a dewatered digested sludge aggregate, at least one of the separation liquid and water obtained in the pretreatment step is mixed with anaerobic digested sludge to dilute the anaerobic digested sludge, The digested sludge agglomerate is smoothly generated by the sludge agglomeration reaction between the digested sludge and the added flocculant, and the amount of the flocculant injected is reduced. Further, in the pretreatment process of the present invention, the aggregated sludge prepared by adding a flocculant is separated into the sludge concentrate and the separated liquid, so that the separated liquid contains water-soluble or hydrophilic useful resources such as phosphorus. As a result, useful resources can be efficiently recovered. Furthermore, since the pretreatment process capable of recovering useful resources is performed before the anaerobic digestion process, phosphorus, siloxane, etc. in the sludge concentrate sent to the anaerobic digestion process are reduced, and the sludge concentration Since it is high concentration, generation | occurrence | production of the deposit containing phosphorus, a siloxane, etc. in an anaerobic digester can be reduced.
本発明において、「％」は、特に言及がない限り、「質量％」を意味する。本発明の嫌気性処理装置は、上記各固有の装置間に汚泥を送るための手段、例えば、配管、ポンプ、バルブ等を適宜、有することができる。 In the present invention, “%” means “% by mass” unless otherwise specified. The anaerobic treatment apparatus of the present invention can appropriately include means for sending sludge between the unique apparatuses, for example, piping, pumps, valves, and the like.
本発明によれば、廃水処理場等での汚泥の嫌気性消化により有機物を分解すると共に、バイオガス（特にメタンガス）を効率良く回収することができ、これよりエネルギー回収効率を著しく向上させることが可能となる。特に、従来の処理方法における大容量の嫌気性消化槽設備を必要とし、消化汚泥処理のための薬品費用が高く、かつ、汚泥が難脱水性で脱水汚泥含水率も下げにくいという技術課題に対し、本発明では低ランニングコストの濃縮装置で汚泥濃度を高く濃縮でき、かつ、嫌気性消化容量も大幅に削減でき、さらには、難脱水性の嫌気性消化汚泥での脱水操作改善も行うことができるため、消化汚泥を効率的に脱水処理することができる低コストの嫌気性消化システムを実現できる。また、本発明は、嫌気性消化槽へのリン、カルシウム、シロキサン等の導入量を従来のほぼ半分に低減でき、ひいては嫌気性消化槽でのリン、カルシウム、シロキサン等を含む析出物の発生を低減でき、嫌気性消化槽及び配管等の維持、管理費用の低減化に寄与するとともにリン等の有用資源を効率的に回収することができる。 According to the present invention, an organic substance can be decomposed by anaerobic digestion of sludge at a wastewater treatment plant or the like, and biogas (especially methane gas) can be efficiently recovered, thereby significantly improving energy recovery efficiency. It becomes possible. In particular, for the technical problem that a large-capacity anaerobic digester equipment in the conventional treatment method is required, the chemical cost for digested sludge treatment is high, and the sludge is difficult to dehydrate and the water content of dehydrated sludge is difficult to reduce. In the present invention, it is possible to concentrate the sludge at a high concentration with a low running cost concentrator, greatly reduce the anaerobic digestion capacity, and further improve the dehydration operation with the hardly dehydrated anaerobic digested sludge. Therefore, a low-cost anaerobic digestion system capable of efficiently dewatering digested sludge can be realized. In addition, the present invention can reduce the amount of phosphorus, calcium, siloxane, and the like introduced into the anaerobic digestion tank to almost half of the conventional amount, and consequently the generation of precipitates containing phosphorus, calcium, siloxane, etc. in the anaerobic digestion tank. This contributes to the maintenance of anaerobic digesters and piping, and the reduction of management costs, and it is possible to efficiently recover useful resources such as phosphorus.
以下、適宜図面を参照しながら、本発明を更に詳細に説明する。 Hereinafter, the present invention will be described in more detail with reference to the drawings as appropriate.
本発明の嫌気性処理方法は、汚泥に凝集剤を添加して調製した凝集汚泥を、汚泥濃度４〜１２wt％の汚泥濃縮物と分離液とに固液分離する前処理工程、該汚泥濃縮物を嫌気性消化するとともにバイオガスを回収する嫌気性消化工程、該嫌気性消化工程で調製された嫌気性消化汚泥に、凝集剤と、前記分離液及び水の少なくとも何れかと、を混合して消化汚泥凝集物を調製する工程、及び該消化汚泥凝集物を固液分離して得られる消化汚泥濃縮物を脱水する工程を含む。 The anaerobic treatment method of the present invention includes a pretreatment step for solid-liquid separation of agglomerated sludge prepared by adding a flocculant to sludge into a sludge concentrate having a sludge concentration of 4 to 12 wt% and a separated liquid, the sludge concentrate Anaerobic digestion step for anaerobic digestion and biogas recovery, anaerobic digestion sludge prepared in the anaerobic digestion step, mixed with a flocculant and at least one of the separation liquid and water for digestion A step of preparing a sludge aggregate, and a step of dehydrating a digested sludge concentrate obtained by solid-liquid separation of the digested sludge aggregate.
本発明において、「汚泥」とは、下水、屎尿、厨芥などの有機性物質を処理する工程で排出される汚泥を意味する。 In the present invention, “sludge” means sludge discharged in a process of treating organic substances such as sewage, manure, and soot.
本発明で処理される汚泥としては、廃水処理設備の最初沈殿池から発生する初沈汚泥と最終沈殿池から発生する余剰汚泥とから選択される少なくとも１種であることが好ましく、両者からの混合汚泥であることが更に好ましい。該汚泥は、貯留槽に貯留され、重力濃縮されることが好ましい。 The sludge to be treated in the present invention is preferably at least one selected from the initial sludge generated from the first settling basin of the wastewater treatment facility and the surplus sludge generated from the final settling basin. More preferably, it is sludge. The sludge is preferably stored in a storage tank and concentrated by gravity.
貯留槽から排出された汚泥に凝集剤が添加され、凝集汚泥が調製される。凝集剤の添加量は、汚泥のＳＳ（Ｓｕｓｐｅｎｄｅｄ Ｓｏｌｉｄｓ、懸濁粒子）に対して０．２〜１．０wt％が好ましく、０．３〜０．６wt％が更に好ましい。 A flocculant is added to the sludge discharged from the storage tank to prepare agglomerated sludge. The amount of the flocculant added is preferably 0.2 to 1.0 wt%, more preferably 0.3 to 0.6 wt%, based on the sludge SS (Suspended Solids, suspended particles).
凝集剤としては、通常用いられる凝集剤を特に限定せずに用いることができる。例えば、ポリ硫酸第二鉄またはＰＡＣ、硫酸バンド等の無機系凝集剤、及び有機高分子凝集剤（以下、高分子凝集剤ともいう）などが挙げられ、各々、単独または組み合わせて用いることができるが、少なくとも高分子凝集剤を含むことが好ましい。高分子凝集剤としては、カチオン系、アニオン系、両性系、等が挙げられ、例えば、アミジン系凝集剤、アクリルアミド系凝集剤、アクリル酸系凝集剤等が挙げられる。 As the flocculant, a commonly used flocculant can be used without particular limitation. Examples thereof include inorganic aggregating agents such as polyferric sulfate or PAC and sulfuric acid bands, and organic polymer aggregating agents (hereinafter also referred to as polymer aggregating agents), and each can be used alone or in combination. Preferably contains at least a polymer flocculant. Examples of the polymer flocculant include cationic, anionic, amphoteric, and the like, and examples thereof include amidine flocculants, acrylamide flocculants, and acrylic acid flocculants.
以下、本発明の嫌気性処理方法を工程別に説明する。 Hereinafter, the anaerobic treatment method of the present invention will be described step by step.
＜前処理工程＞
この前処理工程は、汚泥に凝集剤を添加して調製した凝集汚泥を、汚泥濃度４〜１２wt％の汚泥濃縮物と、分離液と、に固液分離する汚泥濃縮工程である。従来の処理方法では、高分子凝集剤を添加して汚泥を濃縮していたため、３〜４wt％、高くても４〜５wt％程度の汚泥濃度に濃縮することが限界であった。本発明では、汚泥濃度４〜１２wt％までの高濃度化が可能である。一方、分離液には、リン、カルシウム、シロキサン等が含まれる。<Pretreatment process>
This pretreatment process is a sludge concentration process in which the agglomerated sludge prepared by adding a flocculant to sludge is solid-liquid separated into a sludge concentrate having a sludge concentration of 4 to 12 wt% and a separated liquid. In the conventional treatment method, the sludge is concentrated by adding a polymer flocculant, so that the concentration to a sludge concentration of about 3 to 4 wt%, at most about 4 to 5 wt%, is the limit. In the present invention, the concentration can be increased to a sludge concentration of 4 to 12 wt%. On the other hand, the separation liquid contains phosphorus, calcium, siloxane and the like.
＜嫌気性消化工程＞
次に、上記汚泥濃縮物は、嫌気性消化工程に送られ、嫌気性消化されるとともに発生するバイオガスが回収される。汚泥濃縮物の消化は、３０〜６０℃、好ましくは３０〜４０℃の中温消化領域または５０〜６０℃の高温消化領域で行うことが好ましい。嫌気性消化時の好適なｐＨはｐＨ６〜８．５、最も好ましくはｐＨ６．５〜８．０である。<Anaerobic digestion process>
Next, the said sludge concentrate is sent to an anaerobic digestion process, and the biogas generated while anaerobically digesting is collect | recovered. Digestion of the sludge concentrate is preferably carried out in an intermediate temperature digestion region of 30 to 60 ° C, preferably 30 to 40 ° C or a high temperature digestion region of 50 to 60 ° C. A suitable pH during anaerobic digestion is pH 6 to 8.5, most preferably pH 6.5 to 8.0.
油脂成分が多く含まれる後述の有機性廃液または廃棄物を混合消化する場合には、温度が高いほうが中性脂肪や高級脂肪酸の分散性が増すため、５０〜６０℃の高温消化方法を選択することが好ましい。一方、汚泥の嫌気性消化で生成されるアンモニアは高ｐＨと高温域で解離しやすいことから、高温消化ではアンモニア阻害を受けやすくなる点に注意が必要である。消化液中ＮＨ４ ＋−Ｎ濃度としては、中温消化で３，５００ｍｇ／Ｌ以上、高温消化で２，０００ｍｇ／Ｌ以上となるとメタン生成反応が阻害される。これらの操作条件は、濃縮汚泥の汚泥濃度や汚泥性状、嫌気性消化時の水量変動、目標処理水質を加味した上で決定される。When mixing and digesting organic waste liquids or wastes, which will be described later, containing a large amount of oil and fat components, the higher the temperature, the higher the dispersibility of neutral fats and higher fatty acids, so select a high temperature digestion method of 50-60 ° C. It is preferable. On the other hand, since ammonia produced by anaerobic digestion of sludge is easily dissociated at high pH and high temperature, it is necessary to pay attention to the point that ammonia digestion is likely to occur during high temperature digestion. When the NH 4 + -N concentration in the digestive fluid is 3,500 mg / L or more in the medium-temperature digestion and 2,000 mg / L or more in the high-temperature digestion, the methane production reaction is inhibited. These operating conditions are determined in consideration of the sludge concentration and sludge properties of the concentrated sludge, the amount of water during anaerobic digestion, and the target treated water quality.
嫌気性消化工程は、前記汚泥濃縮物を、処理温度３０〜６０℃、ＨＲＴ（水理学的滞留時間：Hydraulic retention time）１〜３日の条件で可溶化および酸発酵処理する前段消化工程と、該前段消化工程で処理された消化汚泥をメタン発酵処理し、嫌気性消化汚泥を調製するメタン発酵工程を含むことがより好ましい。 The anaerobic digestion step is a pre-digestion step in which the sludge concentrate is solubilized and subjected to acid fermentation under the conditions of a treatment temperature of 30 to 60 ° C. and an HRT (Hydraulic retention time) of 1 to 3 days, More preferably, the digested sludge treated in the previous digestion step is subjected to a methane fermentation treatment to prepare an anaerobic digested sludge.
この前段消化工程は、後段のメタン発酵工程の嫌気性処理を促進する機能を有し、メタン発酵工程でのＨＲＴを低減し、バイオガスの回収を効率化・安定化し、粗浮遊物含有率を高く安定に維持し、発酵液粘度を低減するために寄与する。また、前段消化工程でＳＳ濃度の調整を行っても良い。 This pre-stage digestion process has the function of promoting the anaerobic treatment of the post-stage methane fermentation process, reduces the HRT in the methane fermentation process, streamlines and stabilizes the recovery of biogas, and increases the content of crude suspended matter. Maintain high and stable, contribute to reduce the viscosity of fermentation broth. Further, the SS concentration may be adjusted in the previous digestion step.
メタン発酵工程は、処理温度３０〜６０℃、かつＨＲＴ１２〜２０日の条件で行われることが好ましく、ＳＳに対する粗浮遊物含有率が３〜２０％となるように嫌気性消化汚泥が調製されることが好ましい。上記粗浮遊物含有率の粗浮遊物とは、セルロース等の繊維状物質、粒状物質等を意味する。該ＨＲＴは１２〜１５日が更に好ましく、粗浮遊物含有率は５〜１８％が更に好ましい。粗浮遊物含有率を上記範囲とすることにより、消化汚泥濃縮物の脱水性を改善し、脱水ケーキの含水率低減を図ることができる。 The methane fermentation process is preferably performed under the conditions of a processing temperature of 30 to 60 ° C. and HRT of 12 to 20 days, and anaerobic digested sludge is prepared so that the content of crude suspended solids with respect to SS is 3 to 20%. It is preferable. The coarse suspended matter having the above-mentioned coarse suspended solid content means fibrous substances such as cellulose, granular substances and the like. The HRT is more preferably from 12 to 15 days, and the content of crude suspended matters is more preferably from 5 to 18%. By making the crude suspended solid content within the above range, the dewaterability of the digested sludge concentrate can be improved, and the water content of the dewatered cake can be reduced.
また、本発明の嫌気性消化工程では、外部、すなわち、本発明において実施する廃水処理場の系外から搬入した有機性廃液または廃棄物を汚泥とともに処理することができる。外部からの有機性廃液または廃棄物とは、工場、下水処理場等の設備から排出される有機化合物を少なくとも含み、汚泥、草本類等を含んでもよい。外部からの有機性廃液または廃棄物は、前処理工程、前段消化工程及びメタン発酵工程のいずれに搬入してもよい。外部からの有機性廃液または廃棄物を汚泥と一緒に嫌気性消化する場合には、該有機性廃液又は廃棄物のスラリーＴＳ（Total solids）濃度を１〜１５％（更に好ましくは３〜１０％）に調整し、汚泥濃縮物のＴＳに対して１２０％以下（更に好ましくは５〜１００％）のスラリーＴＳ比となる混合条件で添加することが好ましい。ここで、スラリーＴＳ濃度とは、スラリー中のＴＳ濃度を意味し、スラリーＴＳ比とは、スラリーに含まれる搬入物質のＴＳ比率を意味する。スラリーＴＳ濃度は、有機性廃液または廃棄物の種類、濃度、状態、搬入頻度などを加味して決定される。また、外部から搬入される有機性廃液または廃棄物は、必要に応じて物理的、化学的、生物的分解処理された後に嫌気性消化工程に導入されると消化反応を安定化させることができるので好ましい。処理方式の一例としては、湿式破砕、乾式粉砕、熱処理、高温高圧処理、酸またはアルカリ処理、生物的可溶化または酸発酵処理などを好適に挙げることができる。 Moreover, in the anaerobic digestion process of this invention, the organic waste liquid or waste carried in from the outside, ie, the system outside the waste water treatment plant implemented in this invention, can be processed with sludge. The organic waste liquid or waste from the outside includes at least an organic compound discharged from facilities such as factories and sewage treatment plants, and may include sludge, herbs, and the like. The organic waste liquid or waste from the outside may be carried into any of the pretreatment process, the pre-digestion process, and the methane fermentation process. When an organic waste liquid or waste from the outside is subjected to anaerobic digestion together with sludge, the slurry TS (Total solids) concentration of the organic waste liquid or waste is 1 to 15% (more preferably 3 to 10%) ), And it is preferable to add the slurry under a mixing condition that gives a slurry TS ratio of 120% or less (more preferably 5 to 100%) with respect to TS of the sludge concentrate. Here, the slurry TS concentration means the TS concentration in the slurry, and the slurry TS ratio means the TS ratio of the carried-in substance contained in the slurry. The slurry TS concentration is determined in consideration of the type, concentration, state, delivery frequency, etc. of the organic waste liquid or waste. Moreover, the organic waste liquid or waste carried from the outside can stabilize the digestion reaction if it is introduced into the anaerobic digestion step after being subjected to physical, chemical and biological decomposition treatment as necessary. Therefore, it is preferable. As an example of the treatment method, wet crushing, dry pulverization, heat treatment, high-temperature and high-pressure treatment, acid or alkali treatment, biological solubilization or acid fermentation treatment, and the like can be preferably exemplified.
＜消化汚泥凝集物調製工程＞
次に、嫌気性消化工程で調製された嫌気性消化汚泥に凝集剤と、前処理工程の分離液及び水の少なくとも何れかと、を混合して消化汚泥凝集物を調製する。<Digested sludge aggregate preparation process>
Next, the digested sludge aggregate is prepared by mixing the anaerobic digested sludge prepared in the anaerobic digestion step with the flocculant and at least one of the separation liquid and water in the pretreatment step.
嫌気性消化汚泥に添加する凝集剤としては、高分子凝集剤等が好適である。また、ポリ硫酸第二鉄またはＰＡＣ等の無機系凝集助剤と高分子凝集剤の併用も分離液の清澄度を高めるために有効な場合がある。高分子凝集剤としては、高価なアミジン系凝集剤も使用できるが、比較的安価なカチオンポリマー系凝集剤、例えば、アクリル酸エステル系、メタアクリル酸エステル系、アニオン度よりもカチオン度の高い両性系凝集剤等を用いることができる。アクリル酸エステル系としては、分子量が３００〜６００万のものが沈降分離性の高い消化汚泥凝集物を得る上で好ましい。 As the flocculant added to the anaerobic digested sludge, a polymer flocculant or the like is suitable. In addition, the combined use of an inorganic coagulant aid such as polyferric sulfate or PAC and a polymer coagulant may be effective for increasing the clarity of the separated liquid. As the polymer flocculant, an expensive amidine flocculant can be used, but a relatively inexpensive cationic polymer flocculant, for example, acrylate ester-based, methacrylic acid ester-based, amphoteric with higher cationicity than anionic degree A system flocculant or the like can be used. As the acrylic ester, those having a molecular weight of 3 to 6 million are preferable for obtaining a digested sludge aggregate having high sedimentation separation.
凝集剤の添加量は、嫌気性消化汚泥の性状によって変動するが、消化汚泥凝集物の沈降分離性を高めるため、凝集物のフロック径が数ミリ程度になる添加量とすることが好ましい。具体的には、凝集物のフロック径が５〜２０ｍｍの範囲、好ましくは１０〜２０ｍｍの範囲となるように、凝集剤を嫌気性消化汚泥中のＳＳあたり１．０〜２．５％の範囲、好ましくは１．５〜２．０％の範囲で添加する。 The addition amount of the flocculant varies depending on the properties of the anaerobic digested sludge. However, in order to improve the sedimentation and separability of the digested sludge aggregate, it is preferable that the floc diameter of the aggregate is about several millimeters. Specifically, the flocculant has a floc diameter in the range of 5 to 20 mm, preferably in the range of 10 to 20 mm, and the flocculant is in the range of 1.0 to 2.5% per SS in the anaerobic digested sludge. Preferably, it is added in the range of 1.5 to 2.0%.
消化汚泥凝集物調製工程で用いる分離液又は水（「希釈水」ともいう）は、嫌気性消化汚泥を希釈する機能を有する。分離液又は水による濃縮汚泥の希釈により、汚泥の電気伝導度を１２００ｍＳ／ｍ以下、好ましくは７５０ｍＳ／ｍ以下、汚泥のＭアルカリ度を４０００ｍｇ／ｌ以下、好ましくは２５００ｍｇ／ｌ以下、汚泥の温度を３５℃以上、好ましくは５０〜７５℃に調整する。希釈された汚泥の温度は、上記範囲の温度の分離液又は水を添加することによって調整してもよく、あるいは添加後に加熱してもよい。希釈水は、前処理工程で得られる分離液、通常の飲用水等の他、溶解成分等の濃度が比較的小さい等の水質条件（電気伝導度５００ｍＳ／ｍ以下、Ｍアルカリ度１５００ｍｇ／Ｌ以下、ＳＳ１５００ｍｇ／Ｌ以下、ＣＯＤＣｒ１５０００ｍｇ／Ｌ以下）を満たす水であれば処理プラント内のどのプロセス水を使用しても良い。また、活性汚泥処理水、生物脱臭装置廃液といった生物処理水を使用することも可能である。 The separation liquid or water (also referred to as “diluted water”) used in the digested sludge aggregate preparation step has a function of diluting anaerobic digested sludge. By diluting the concentrated sludge with the separation liquid or water, the electrical conductivity of the sludge is 1200 mS / m or less, preferably 750 mS / m or less, the M alkalinity of the sludge is 4000 mg / l or less, preferably 2500 mg / l or less, and the sludge temperature. Is adjusted to 35 ° C. or higher, preferably 50 to 75 ° C. The temperature of the diluted sludge may be adjusted by adding a separation liquid or water having a temperature in the above range, or may be heated after the addition. Dilution water is a water quality condition (electric conductivity of 500 mS / m or less, M alkalinity of 1500 mg / L, etc.) in addition to the separation liquid obtained in the pretreatment step, normal drinking water, etc. Hereinafter, any process water in the treatment plant may be used as long as it satisfies SS 1500 mg / L or less and COD Cr 15000 mg / L or less). It is also possible to use biologically treated water such as activated sludge treated water and biological deodorizing apparatus waste liquid.
得られた消化汚泥凝集物を固液分離して消化汚泥濃縮物と分離液とを調製する。消化汚泥濃縮物の濃縮倍率は２．５〜８倍程度が好ましい。ここで、濃縮倍率とは、消化汚泥凝集物の容積を消化汚泥濃縮物の容積で除した値を意味する。 The digested sludge aggregate obtained is subjected to solid-liquid separation to prepare a digested sludge concentrate and a separated liquid. The concentration rate of the digested sludge concentrate is preferably about 2.5 to 8 times. Here, the concentration ratio means a value obtained by dividing the volume of the digested sludge aggregate by the volume of the digested sludge concentrate.
固液分離された消化汚泥濃縮物に、再び、凝集剤及び必要に応じて希釈水を添加して再濃縮凝集汚泥を調製する。この際用いられる凝集剤及び希釈水は、消化汚泥凝集物調製工程で用いる凝集剤及び希釈水でよい。再濃縮凝集汚泥が、十分な脱水性を有する場合（濃縮凝集汚泥のＴＳ濃度として４〜１５ｗｔ％の範囲、好ましくは６〜１０ｗｔ％）は、最終的な消化汚泥凝集物として脱水工程に送る。しかし、該再濃縮凝集汚泥が十分な脱水性を有しない場合、又は当初の設計上必要とされる場合（濃縮凝集汚泥のＴＳ濃度として４ｗｔ％未満の場合）等は、例えば、上記凝集剤再注入とそれに続く固液分離又は固液分離のみを繰り返してもよい。凝集剤再注入に用いる凝集剤は、消化汚泥凝集物調製工程において用いた凝集剤と同じ凝集剤を用いてもよいし、異なる凝集剤を用いてもよい。 To the digested sludge concentrate that has been subjected to solid-liquid separation, a flocculant and, if necessary, dilution water are added again to prepare a reconcentrated flocculent sludge. The flocculant and dilution water used at this time may be the flocculant and dilution water used in the digested sludge aggregate preparation step. When the re-concentrated coagulated sludge has sufficient dewatering property (the TS concentration of the concentrated coagulated sludge is in the range of 4 to 15 wt%, preferably 6 to 10 wt%), it is sent to the dehydration process as the final digested sludge aggregate. However, when the reconcentrated flocculated sludge does not have sufficient dewaterability, or when it is required in the original design (when the TS concentration of the concentrated flocculated sludge is less than 4 wt%), Only injection and subsequent solid-liquid separation or solid-liquid separation may be repeated. As the flocculant used for reinjection of the flocculant, the same flocculant as that used in the digested sludge aggregate preparation step may be used, or a different flocculant may be used.
最終的な消化汚泥凝集物は、後段の脱水工程におけるせん断力を受けた後もその粒状のフロック形状がわずかに残る程度の強度を持つフロックであることが好ましい。このような消化汚泥凝集物を得るための凝集剤としては、特に限定されるべきものではないが、高分子凝集剤が好ましい。高分子凝集剤としては、上記凝集汚泥調製工程に使用するものが挙げられ、前処理工程の凝集剤と同一でも異なっていてもよい。 The final digested sludge agglomerate is preferably a floc having such a strength that the granular floc shape remains slightly even after receiving a shearing force in the subsequent dewatering step. The flocculant for obtaining such a digested sludge aggregate is not particularly limited, but a polymer flocculant is preferable. Examples of the polymer flocculant include those used in the above-mentioned flocculent sludge preparation step, and may be the same as or different from the flocculant in the pretreatment step.
＜脱水工程＞
次に、消化汚泥凝集物を脱水して、脱水ケーキと分離液に固液分離す。本発明において、脱水ケーキの濃縮倍率は４〜１０倍程度が好ましい。ここで、濃縮倍率とは、消化汚泥凝集物の容積を脱水ケーキの容積で除した値を意味する。脱水ケーキ調製工程で分離された分離液は、ＳＳ濃度、Ｍアルカリ度、及び電気伝導度が小さいため、消化汚泥凝集物を調製する工程で使用する希釈水として好適である。脱水ケーキは、低含塩かつ低含水率であるため、再資源化が可能であり、コンポスト化、炭化、燃料化などの二次加工等にも好適である。<Dehydration process>
Next, the digested sludge aggregate is dehydrated and separated into a dehydrated cake and a separated liquid. In the present invention, the concentration rate of the dehydrated cake is preferably about 4 to 10 times. Here, the concentration ratio means a value obtained by dividing the volume of the digested sludge aggregate by the volume of the dewatered cake. The separated liquid separated in the dehydrated cake preparation step has a low SS concentration, M alkalinity, and electrical conductivity, and is therefore suitable as dilution water used in the step of preparing digested sludge aggregates. Since the dehydrated cake has a low salt content and a low water content, it can be recycled, and is suitable for secondary processing such as composting, carbonization, and fueling.
＜リン及びシロキサン回収＞
前処理工程で得られる分離液には、リン、カルシウム、シロキサン等が含まれている。本発明では、これらを含む分離液のすべて又は一部をリン、カルシウム、シロキサン等を回収乃至除去する工程に送ることができる。リンの回収には、ヒドロキシアパタイトを用いる接触脱リン法、リン酸マグネシウムアンモニウムを用いるＭＡＰ法等が適用できる。<Phosphorus and siloxane recovery>
The separation liquid obtained in the pretreatment step contains phosphorus, calcium, siloxane and the like. In the present invention, all or a part of the separation liquid containing them can be sent to a step of recovering or removing phosphorus, calcium, siloxane and the like. For recovery of phosphorus, a catalytic dephosphorization method using hydroxyapatite, a MAP method using magnesium ammonium phosphate, or the like can be applied.
ＭＡＰ法では、反応槽、例えば、上向流槽内に予めＭＡＰの種晶を充填し、また、所望により不足するＭＡＰ成分を補うための薬剤、例えば、ＭｇＣｌ２、Ｍｇ（ＯＨ）２等を分離液に添加し、更に、所望により分離液のｐＨを７．８〜８．５に調整して、分離液を上向流で反応槽に通水し、ＭＡＰの粒径を増大させ、この増大した粒径を有するＭＡＰを適宜、反応槽から抜き出し、分離・回収する方法が挙げられる。反応槽で生成した微細なＭＡＰは槽上部から回収し、反応槽に戻される。In the MAP method, a seed tank of MAP is preliminarily filled in a reaction tank, for example, an upward flow tank, and an agent such as MgCl 2 , Mg (OH) 2 or the like for supplementing the MAP component which is insufficient if desired is added. The pH of the separation liquid is adjusted to 7.8 to 8.5 as desired, and the separation liquid is passed through the reaction vessel in an upward flow to increase the particle size of MAP. A method of appropriately extracting MAP having an increased particle size from the reaction vessel and separating / recovering it can be mentioned. Fine MAP generated in the reaction tank is recovered from the upper part of the tank and returned to the reaction tank.
シロキサンの回収は、分離液をガス乃至噴霧状として、又はそのままの状態で、活性炭、シリカゲル、ゼオライト、ポリマー（例えば、スチレン・ジビニルベンゼン共重合体等）等の吸着剤により、吸着させる方法により行うことができる。また、所望により窒素ガスを、適宜、加温して、シロキサンを吸着した吸着剤に通すことにより、シロキサンを脱離、回収することもできる。後述のバイオガスに対しても上記と同様の吸着剤を用いてシロキサンを処理することが可能であり、同様の方法でシロキサンを脱離、回収することができる。 Siloxane is recovered by a method in which the separated liquid is adsorbed with an adsorbent such as activated carbon, silica gel, zeolite, polymer (for example, styrene / divinylbenzene copolymer) in the form of gas or spray or as it is. be able to. Moreover, siloxane can also be desorbed and recovered by optionally heating nitrogen gas as appropriate and passing it through an adsorbent adsorbing siloxane. It is possible to treat siloxane with biogas described later using the same adsorbent as described above, and siloxane can be desorbed and recovered by the same method.
本発明は、上述のように分離液と汚泥濃縮物に固液分離する工程を有するため、嫌気性消化装置へのリン、シロキサン等の導入量が従来よりも低減し、ひいては同装置でのリン、シロキサン等を含む析出物の発生が低減し、同装置又は配管等の維持、管理費用の低減化に寄与する効果がある。 Since the present invention has the step of solid-liquid separation into the separation liquid and the sludge concentrate as described above, the amount of phosphorus, siloxane, and the like introduced into the anaerobic digester is reduced compared to the prior art, and consequently the phosphorus in the apparatus is reduced. This reduces the generation of precipitates containing siloxane and the like, and has the effect of contributing to the maintenance of the apparatus or piping and the reduction of management costs.
＜嫌気性処理装置＞
本発明の嫌気性処理装置は、汚泥に凝集剤を添加して凝集汚泥を調製する凝集槽、汚泥濃度４〜１２wt％の汚泥濃縮物と分離液とに固液分離する前処理汚泥濃縮装置、該汚泥濃縮物を嫌気性消化するとともにバイオガスを回収する嫌気性消化装置、該嫌気性消化装置で調製された嫌気性消化汚泥に、凝集剤と、前記分離液及び水の少なくとも何れかと、を混合して消化汚泥凝集物を調製する消化汚泥凝集装置、及び該消化汚泥凝集物を固液分離して得られる消化汚泥濃縮物を脱水する装置を含む。<Anaerobic treatment device>
The anaerobic treatment apparatus of the present invention is a coagulation tank for adding coagulant to sludge to prepare coagulated sludge, a pretreatment sludge concentration apparatus for solid-liquid separation into a sludge concentrate having a sludge concentration of 4 to 12 wt% and a separated liquid, Anaerobic digester that anaerobically digests the sludge concentrate and collects biogas, anaerobic digested sludge prepared by the anaerobic digester, a flocculant, and at least one of the separation liquid and water. A digested sludge agglomeration apparatus for preparing a digested sludge agglomerate by mixing, and an apparatus for dewatering a digested sludge concentrate obtained by solid-liquid separation of the digested sludge agglomerate are included.
凝集槽は、通常用いられる凝集槽でよい。 The aggregation tank may be a commonly used aggregation tank.
前処理汚泥濃縮装置は、凝集汚泥を汚泥濃縮物と分離液とに固液分離する固液分離槽でよい。固液分離槽としては、特に限定されず、重力濃縮法が適用される単なる槽、遠心濃縮法が適用される遠心分離機、浮上濃縮法が適用される分離機、スクリーンを用いた分離機、スリット型濃縮機等が挙げられる。中でも、スリット型濃縮機は好ましく、例えば、前記特開２００３−２１１２９３号公報（特許文献３）に記載の、処理物をスリット板で受け止め、多数のスリットを形成したスリット板上に周面を突出せしめた多数の円板が、処理物排出方向に回転軸により偏心回転することによって、処理物はスリット板上を排出側に送られ、この過程でスリット内の円板との隙間から液体成分が落下して濾過され、処理物中の固体成分は分離捕集され、さらにスリット板の上面に近接して処理物の排出方向に回転し、スリット板上の捕集物を圧搾して脱液するベルトコンベアを上記スリット板上に設けた機械構造が挙げられる。スリット型濃縮機を適用すると、安価なランニングコストで安定して確実に４〜１２wt％の高濃度化が可能である。 The pretreatment sludge concentration apparatus may be a solid-liquid separation tank that separates the aggregated sludge into a sludge concentrate and a separated liquid. The solid-liquid separation tank is not particularly limited, but a simple tank to which the gravity concentration method is applied, a centrifugal separator to which the centrifugal concentration method is applied, a separator to which the floating concentration method is applied, a separator using a screen, A slit type concentrator can be used. Among them, the slit type concentrator is preferable. For example, as described in Japanese Patent Application Laid-Open No. 2003-2111293 (Patent Document 3), the processed product is received by the slit plate, and the peripheral surface protrudes on the slit plate in which a large number of slits are formed. A large number of squeezed discs are eccentrically rotated by the rotating shaft in the direction of discharge of the processed material, so that the processed material is sent to the discharge side on the slit plate, and in this process, the liquid component is released from the gap with the disk in the slit. It is dropped and filtered, and the solid components in the processed material are separated and collected, and further rotated in the direction of discharge of the processed material close to the upper surface of the slit plate, and the collected material on the slit plate is squeezed and dehydrated. The mechanical structure which provided the belt conveyor on the said slit board is mentioned. When a slit type concentrator is applied, a high concentration of 4 to 12 wt% can be stably and reliably achieved at an inexpensive running cost.
嫌気性消化装置は、少なくとも嫌気性消化槽を含む。嫌気性消化槽としては、特に限定されないが、完全混合型消化槽を適用することが好ましい。嫌気性消化槽は、槽内液の均質化や温度分布の均一化とともに、スカムの発生を防止するために攪拌が必須であり、本発明では機械攪拌方式が最も効率的であるが、設備環境や処理条件に応じてポンプ攪拌方式、ガス攪拌方式を付属することも効果的である。さらに、これらの要件を備えた水密かつ気密な構造の消化槽であれば鉄筋コンクリート造りまたは鋼板製のいずれでも良く、既設の嫌気性消化槽を処理条件に合わせて改造・更新することでも適用可能である。また、嫌気性消化装置は、汚泥濃縮物を可溶化および酸発酵処理する可溶化・酸発酵処理槽と、該槽で処理された消化汚泥をメタン発酵処理するメタン発酵槽と、を含む構成とすることが好ましい。嫌気性消化装置は、外部からの有機性廃液または廃棄物を貯留する外部バイオマス貯留装置と、該外部バイオマス貯留装置から排出されるバイオマスを、前記貯留装置、可溶化および酸発酵処理する装置、及びメタン発酵装置からなる群から選択される少なくとも１つに導入する機構及び配管を含むことが好ましい。 The anaerobic digester includes at least an anaerobic digester. Although it does not specifically limit as an anaerobic digester, It is preferable to apply a complete mixing type digester. In an anaerobic digestion tank, in addition to homogenization of the liquid in the tank and uniform temperature distribution, stirring is essential to prevent the occurrence of scum, and in the present invention, the mechanical stirring system is the most efficient, but the equipment environment It is also effective to attach a pump stirring method and a gas stirring method according to the processing conditions. Furthermore, any water-tight and air-tight digester with these requirements can be either reinforced concrete or steel plate, and it can also be applied by modifying or updating an existing anaerobic digester according to the processing conditions. is there. The anaerobic digester includes a solubilization / acid fermentation treatment tank for solubilizing and acid fermentation treatment of the sludge concentrate, and a methane fermentation tank for subjecting the digested sludge treated in the tank to methane fermentation treatment. It is preferable to do. The anaerobic digester includes an external biomass storage device for storing organic waste liquid or waste from the outside, a device for solubilizing and acid fermentation treatment of the biomass discharged from the external biomass storage device, and It is preferable to include a mechanism and piping for introduction into at least one selected from the group consisting of methane fermentation apparatuses.
消化汚泥凝集装置は、消化汚泥凝集槽と、適宜、希釈した汚泥を導入する手段、凝集剤添加手段、攪拌手段、加温手段、凝集汚泥の引き抜き手段等を備える。また、別途、希釈のための配管内混合装置を具備していてもよい。 The digested sludge aggregating apparatus includes a digested sludge aggregating tank, a means for introducing diluted sludge as appropriate, a coagulant adding means, a stirring means, a heating means, a means for extracting the coagulated sludge, and the like. In addition, an in-pipe mixing device for dilution may be provided separately.
本発明の嫌気性処理装置は、消化汚泥凝集物から消化汚泥濃縮物を調製する装置を具備することが好ましい。 The anaerobic treatment apparatus of the present invention preferably includes an apparatus for preparing a digested sludge concentrate from the digested sludge aggregate.
消化汚泥濃縮物を調製する装置は、凝集剤により凝集汚泥を調製する汚泥凝集処理装置、該凝集汚泥を固液分離して濃縮凝集汚泥を調製する凝集汚泥分離濃縮装置、該濃縮凝集汚泥に凝集剤を添加して再濃縮凝集汚泥を調製する装置を備えることが好ましい。 The apparatus for preparing the digested sludge concentrate is a sludge aggregating treatment apparatus for preparing agglomerated sludge with a coagulant, agglomerated sludge separating and concentrating apparatus for preparing the agglomerated sludge by solid-liquid separation of the agglomerated sludge, and agglomerating the concentrated agglomerated sludge. It is preferable to provide an apparatus for preparing the reconcentrated agglomerated sludge by adding an agent.
凝集汚泥分離濃縮装置は、凝集汚泥を濃縮凝集汚泥と分離液に固液分離する装置である。凝集汚泥分離濃縮装置は、特に限定されず、重力濃縮法が適用される単なる槽、遠心濃縮法が適用される遠心分離機、浮上濃縮法が適用される分離機、スクリーンを用いた分離機等が挙げられる。中でも、スクリーンを備えた固液分離装置が好ましく、例えば、一定間隔で平行に並ぶ複数のスクリーンと隣り合う該スクリーンの間で回転する複数の円盤により隣り合う該スクリーン間の隙間の凝集汚泥を物理的に排除するとともに濃縮凝集汚泥と分離水とに分別することが可能な固液分離装置が挙げられる。ここで、スクリーンのスリット幅は原理的に消化汚泥凝集物のフロック径未満であり、０.１〜２．５ｍｍが好ましい。 The agglomerated sludge separation / concentration device is a device that separates the agglomerated sludge into concentrated agglomerated sludge and a separated liquid. The coagulation sludge separation and concentration device is not particularly limited, and is simply a tank to which the gravity concentration method is applied, a centrifugal separator to which the centrifugal concentration method is applied, a separator to which the floating concentration method is applied, a separator using a screen, etc. Is mentioned. Among them, a solid-liquid separation device provided with a screen is preferable. For example, agglomerated sludge in a gap between adjacent screens is physically separated by a plurality of disks rotating in parallel with a plurality of screens arranged in parallel at regular intervals. And a solid-liquid separation device that can be separated into concentrated agglomerated sludge and separated water. Here, the slit width of the screen is in principle less than the floc diameter of the digested sludge aggregate, and is preferably 0.1 to 2.5 mm.
再濃縮凝集汚泥調製装置は、適宜、濃縮凝集汚泥導入手段、凝集剤添加手段、攪拌手段、再濃縮凝集汚泥の引き抜き手段等を備える。 The reconcentrated agglomerated sludge preparation apparatus appropriately includes a concentrated agglomerated sludge introduction unit, a flocculant addition unit, a stirring unit, a reconcentrated agglomerated sludge extraction unit, and the like.
消化汚泥濃縮物を脱水する装置は、特に限定されず、通常、凝集汚泥分離濃縮装置と原理的に同じものを用いることができるが、凝集汚泥分離濃縮装置よりも脱水ケーキを分離するための消化汚泥凝集物への応力は高くすることが一般的であり、公知手段を用いることができる。脱水ケーキ調製装置は、再濃縮凝集汚泥へ応力を付与する手段と分離液を透過し、消化汚泥凝集物を保持するろ過手段から構成されることが好ましい。消化汚泥凝集物へ応力を付与する手段としては、プレス、遠心等が挙げられる。ろ過手段としては、開孔径が０．１〜２．５ｍｍのスクリ−ン等が挙げられる。 The apparatus for dewatering the digested sludge concentrate is not particularly limited. Usually, the same apparatus as the agglomerated sludge separation and concentration apparatus can be used, but the digestion for separating the dehydrated cake than the agglomerated sludge separation and concentration apparatus is possible. Generally, the stress on the sludge aggregate is increased, and publicly known means can be used. The dewatered cake preparation device is preferably composed of a means for applying stress to the reconcentrated agglomerated sludge and a filtering means for permeating the separated liquid and holding the digested sludge agglomerates. Examples of means for applying stress to the digested sludge aggregate include press and centrifugation. Examples of the filtering means include a screen having an opening diameter of 0.1 to 2.5 mm.
次に、本発明の一例を、図を参照して更に説明する。 Next, an example of the present invention will be further described with reference to the drawings.
図１は、本発明の第一の実施形態を示すブロックフロー図で、嫌気性処理装置の構成を表す説明図である。 FIG. 1 is a block flow diagram showing a first embodiment of the present invention, and is an explanatory diagram showing a configuration of an anaerobic treatment apparatus.
汚泥１は、貯留装置２に送られる。次いで、汚泥１は、貯留装置２から排出され、配管を介して凝集槽３に送られる。凝集槽３において、汚泥１に凝集剤４が添加されて、凝集汚泥５が調製される。凝集汚泥５は、前処理汚泥濃縮槽６に送られ、汚泥濃度４〜１２％の汚泥濃縮物７と分離液８とに固液分離される。汚泥濃縮物７は、嫌気性消化装置９に送られ、汚泥の嫌気性消化によりバイオガス１０及び嫌気性消化汚泥１１を生成する。バイオガス１０は、バイオガスタンク１０１に送られ、次いでバイオガス１０は、ガス利用設備１０２（例えば、ガスタービン、バイオガスボイラ、ガス燈、乾燥機熱源等）、あるいは余剰ガス燃焼装置１０３に送られる。嫌気性消化汚泥１１は、消化汚泥凝集装置１２に送られる。消化汚泥凝集装置１２には、前処理汚泥濃縮槽６にて形成される分離液８の一部が導入される。消化汚泥凝集装置１２において、嫌気性消化汚泥１１に分離液８と凝集剤１３が添加され、消化汚泥凝集物１５と分離液１４が形成される。消化汚泥凝集装置１２からの消化汚泥凝集物１５は、脱水装置１６に送られ、分離液１７を分離するとともに脱水ケーキ１８が調製される。分離液８の一部、分離液１４、及び分離液１７は、リン回収等の廃水処理設備１０４等に送られる。なお、バイオガスタンクの前にシロキサン除去乃至回収装置を設けても良い。
The sludge 1 is sent to the
次に図２は、本発明の第二の実施形態を示すブロックフロー図で、嫌気性処理装置の構成を表す説明図であり、嫌気性消化の前段で可溶化および酸発酵処理を行うものである。 Next, FIG. 2 is a block flow diagram showing a second embodiment of the present invention, which is an explanatory diagram showing the configuration of the anaerobic treatment apparatus, and performs solubilization and acid fermentation treatment before anaerobic digestion. is there.
図１のフローにおいて、前処理泥濃縮槽６にて分離された汚泥濃縮物７は、嫌気性消化装置８に送られる前に可溶化および酸発酵処理装置９ａに送られ、可溶化および酸発酵処理が施された消化汚泥７ａが生成される。消化汚泥７ａは、嫌気性消化装置９に送られ、以降は図１のフローに従って、処理される。
In the flow of FIG. 1, the sludge concentrate 7 separated in the pretreatment mud concentration tank 6 is sent to the solubilization and acid
次に図３は、本発明の第三の実施形態を示すブロックフロー図で、嫌気性処理装置の構成を表す説明図であり、嫌気性消化汚泥の凝集剤による汚泥凝集処理を２回に分割して行うものである。 Next, FIG. 3 is a block flow diagram showing a third embodiment of the present invention, which is an explanatory diagram showing the configuration of the anaerobic treatment apparatus, and divides the sludge agglomeration treatment by an aerobic digested sludge flocculant into two times. It is what you do.
本フローでは、図２のフローにおいて、嫌気性消化汚泥１１及び分離液８の一部が、消化汚泥凝集槽１２に送られ、添加される凝集剤１３により分離液１４を分離するとともに消化汚泥凝集物１５が調製される工程を以下のように変更する。
In this flow, in the flow of FIG. 2, anaerobic digested
嫌気性消化汚泥１１及び分離液８の一部は、汚泥凝集処理装置１２ａに送られ、添加される凝集剤１３ａにより凝集汚泥１２ｃが調製される。凝集汚泥１２ｃは、凝集汚泥分離濃縮装置１４Ａに導入され、分離液１４と濃縮凝集汚泥１２ｄに固液分離される。次いで、濃縮凝集汚泥１２ｄは、再濃縮凝集汚泥調製装置１２ｂに送られ、添加される凝集剤１３ｂにより再濃縮凝集汚泥が調製され、これを最終的な消化汚泥凝集物１５とする。
The anaerobic digested
次に図４は、本発明の第四の実施形態を示すブロックフロー図で、嫌気性処理装置の構成を表す説明図であり、図３のフローにおいて、汚泥凝集処理装置１２ａに生物処理水１９を添加して汚泥を希釈するものであり、他の処理は、図３と同じである。
Next, FIG. 4 is a block flow diagram showing the fourth embodiment of the present invention and is an explanatory diagram showing the configuration of the anaerobic treatment device. In the flow of FIG. 3, the biologically treated
この生物処理水としては、活性汚泥処理水、生物脱臭処理水、硝化脱窒処理水等が挙げられる。生物処理水の含有成分の種類、及びその濃度は、凝集剤の種類又は添加量、ひいては費用に影響するため、処理目的に応じて、適宜決定される。 Examples of the biologically treated water include activated sludge treated water, biological deodorized treated water, and nitrification / denitrification treated water. The kind and concentration of the biologically treated water component are appropriately determined depending on the purpose of treatment because they affect the kind or amount of the flocculant and the cost.
次に図５は、本発明の第五の実施形態を示すブロックフロー図で、嫌気性処理装置の構成を表す説明図であり、図４のフローにおいて、外部から搬入した有機性廃液または廃棄物も嫌気性消化処理を行うものであり、他の処理は、図４と同じである。 Next, FIG. 5 is a block flow diagram showing the fifth embodiment of the present invention and is an explanatory diagram showing the configuration of the anaerobic treatment apparatus. In the flow of FIG. 4, the organic waste liquid or waste carried from the outside is shown. Is an anaerobic digestion process, and the other processes are the same as those in FIG.
本フローでは、有機性廃液または廃棄物２０は、スラリーとしてバイオマス貯槽２１に貯留される。バイオマス貯槽２１からのスラリー２２は、所望によりＴＳ濃度を調整した後、貯留槽２、可溶化および酸発酵処理装置９ａ、及び嫌気性消化装置９の少なくとも何れかに導入され、処理が施される。
In this flow, the organic waste liquid or
上記図１〜５の嫌気性処理装置は、自動制御であってよいし、バッチ処理であってもよいし、その組み合わせであってもよい。また、各種汚泥の温度制御も自動化してもよい。 The anaerobic processing apparatus of FIGS. 1 to 5 may be automatic control, batch processing, or a combination thereof. In addition, temperature control of various sludges may be automated.
以下、本発明の実施例を説明する。Ａ下水処理場から発生した下水汚泥について、本発明の嫌気性処理試験を行った。なお、本発明はこの実施例により何等制限されるものではない。 Examples of the present invention will be described below. The sewage sludge generated from the A sewage treatment plant was subjected to the anaerobic treatment test of the present invention. In addition, this invention is not restrict | limited at all by this Example.
試験では汚泥にカチオン性高分子凝集剤（平均分子量３００万）を０．４％（対ＳＳ比）添加混合して凝集処理後、背圧板付き機械濃縮機で汚泥濃縮物と分離液とに固液分離した。表１に汚泥、汚泥濃縮物、分離液の性状を示す。 In the test, 0.4% (with respect to SS ratio) of cationic polymer flocculant (average molecular weight: 3 million) was added to sludge and mixed, and then the sludge concentrate and the separated liquid were solidified with a mechanical concentrator with a back pressure plate. The liquid was separated. Table 1 shows the properties of sludge, sludge concentrate, and separation liquid.
表２に嫌気性消化装置における嫌気性消化試験条件を示す。嫌気性処理試験では、耐熱塩化ビニル製の完全混合型消化試験装置（総容積３０Ｌ、有効容積２５Ｌ、ジャケット温水循環式）を用いた。また、可溶化および酸発酵装置では、東京理化器械（株）製ジャーファーメンターＭＤＬを用いた（総容積１０Ｌの完全混合型、４Ｌ水深で運転）。試験では、嫌気性消化装置（消化槽）は３７℃、可溶化及び酸発酵装置（可溶化槽）では４５℃で運転した。なお、比較例２では５５℃の高温嫌気性処理試験を行った。原料投入は、チューブポンプＲＰ−６０型（東京理化器械株式会社製）を用い、１日あたり４〜８回に分けてタイマー制御で投入した。 Table 2 shows the anaerobic digestion test conditions in the anaerobic digester. In the anaerobic treatment test, a completely mixed digestion test apparatus (total volume 30 L, effective volume 25 L, jacket hot water circulation type) made of heat-resistant vinyl chloride was used. In the solubilization and acid fermentation apparatus, a jar fermenter MDL manufactured by Tokyo Rika Kikai Co., Ltd. was used (fully mixed type with a total volume of 10 L, operated at a depth of 4 L). In the test, the anaerobic digester (digestion tank) was operated at 37 ° C, and the solubilization and acid fermentation apparatus (solubilization tank) was operated at 45 ° C. In Comparative Example 2, a high temperature anaerobic treatment test at 55 ° C. was performed. The raw material was charged using a tube pump RP-60 type (manufactured by Tokyo Rika Kikai Co., Ltd.) in 4 to 8 times per day with a timer control.
［実施例１］
図１のフローに従って、実施した。[Example 1]
It implemented according to the flow of FIG.
［実施例２］
図２のフローに従って、実施した。なお、嫌気消化汚泥の脱水処理については、図３と図４に示す処理方法も併せて行った。[Example 2]
It implemented according to the flow of FIG. In addition, about the dehydration process of anaerobic digestion sludge, the processing method shown in FIG. 3 and FIG. 4 was also combined.
［比較例］
図６のフローに従って、実施した。なお、消化汚泥凝集物１５は、高分子凝集剤による汚泥凝集により調製した。[Comparative example]
It implemented according to the flow of FIG. The digested
なお、分析方法は下記の方法で行った。
・TS（Total solids、全蒸発残留物）；105℃蒸発残留物重量（JIS K 0102）
・VTS（Volatile total solids、強熱減量）；600℃強熱減量（JIS K 0102）
・SS（Suspended solids、懸濁粒子）；遠心分離法による回転数3,000rpm,10分間での沈殿物重量（JIS K 0102）
・VSS（Volatile suspended solids、揮発性懸濁粒子）；懸濁粒子の600℃強熱減量（JIS K 0102）
・CODCr（化学的酸素消費量）；重クロム酸カリウム法（JIS K 0102）
・BOD（生物化学的酸素消費量）；ウインクラー・アジ化ナトリウム変法（JIS K 0102）
・タンパク質；（ケルダール窒素−アンモニア性窒素）×6.25
・揮発性有機酸（VFA）；高速液体クロマトグラフ（エルマ光学ERC-8710、検出器 RI、カラムShodex RSpak KC-811、カラム温度60℃、移動相0.1％りん酸）
・メタンガス、炭酸ガス；ガスクロマトグラフ（GLサイエンスGC-323、検出器TCD、TCD電流値120A、分離カラム Active Carbon 30/60、カラム温度 95℃、キャリアガス He）
・消化ガス中のシロキサン：消化ガスを流通速度0.6L／分でヘキサン溶液に通液させてシロキサンを捕集後、濃縮してガスクロマトグラフ質量分析計GC/MSで定量分析。ここでは、下水汚泥消化ガス中に最も多く含まれるとされる環状シロキサンのデカメチルシクロペンタシロキサン（D5）濃度を定量分析により評価。
・溶解性画分；GF/B（1μm）でのろ液
・Ｍアルカリ度；遠心分離機による回転数3,000rpm、3分間での上澄液を0.1mol/Lの塩酸溶液でpH4.8まで滴定（下水試験方法）
・粗浮遊物；呼び寸法７４μｍふるいでの粗浮遊物分析（下水試験方法）The analysis method was as follows.
-TS (Total solids): 105 ° C evaporation residue weight (JIS K 0102)
・ VTS (Volatile total solids, loss on ignition); 600 ° C loss on ignition (JIS K 0102)
・ SS (Suspended solids, suspended particles): 3,000rpm, sediment weight in 10 minutes by centrifugation (JIS K 0102)
・ VSS (Volatile suspended solids); Loss on ignition of suspended particles at 600 ℃ (JIS K 0102)
・ COD Cr (chemical oxygen consumption); potassium dichromate method (JIS K 0102)
・ BOD (Biochemical Oxygen Consumption); Winkler ・ Modified Sodium Azide (JIS K 0102)
・ Protein; (Kjeldahl nitrogen-ammoniacal nitrogen) x 6.25
・ Volatile organic acid (VFA); High performance liquid chromatograph (Elmer Optics ERC-8710, detector RI, column Shodex RSpak KC-811, column temperature 60 ° C, mobile phase 0.1% phosphoric acid)
・ Methane gas, carbon dioxide gas chromatograph (GL Science GC-323, detector TCD, TCD current value 120A, separation column Active Carbon 30/60, column temperature 95 ℃, carrier gas He)
Siloxane in digestion gas: Digestion gas is passed through a hexane solution at a flow rate of 0.6 L / min to collect siloxane, and then concentrated and quantitatively analyzed with a gas chromatograph mass spectrometer GC / MS. Here, the decamethylcyclopentasiloxane (D5) concentration of cyclic siloxane, which is said to be the most abundant in sewage sludge digestion gas, was evaluated by quantitative analysis.
・ Solubility fraction: Filtrate in GF / B (1 μm) ・ M alkalinity: 3,000 rpm, 3 minutes of supernatant with 0.1 mol / L hydrochloric acid solution to pH 4.8 Titration (sewage test method)
・ Coarse suspended solids; analysis of coarse suspended solids with a nominal size of 74 μm (sewage test method)
表３の嫌気性処理試験結果に示すように、実施例１及び２による嫌気性処理では従来技術と同等のＴＳ分解率、ＶＴＳ分解率、メタンガス発生率の性能が出ていることがわかる。 As shown in the anaerobic treatment test results in Table 3, it can be seen that the anaerobic treatments according to Examples 1 and 2 have the same performance of TS decomposition rate, VTS decomposition rate, and methane gas generation rate as those of the prior art.
また、消化ガス中のシロキサンＤ５濃度を比較すると、実施例１と２において含有率が低くなっており、高濃度に保持された消化汚泥ＳＳ分にシロキサン化合物が吸着されることで消化ガス中へのシロキサン濃度が低くなったものと考えられる。 Moreover, when the siloxane D5 density | concentration in digestion gas is compared, the content rate is low in Example 1 and 2, and a siloxane compound is adsorbed by digestion sludge SS content hold | maintained at high density | concentration into digestion gas It is considered that the concentration of siloxane in the solution was lowered.
さらに、粗浮遊物を比較すると、実施例１と２において含有率が高くなっており、従来の消化汚泥よりも汚泥脱水には有利な汚泥条件となっていることがわかる。 Furthermore, when the coarse suspended matters are compared, it can be seen that the contents are higher in Examples 1 and 2, and the sludge conditions are more advantageous for sludge dewatering than the conventional digested sludge.
なお、比較例、実施例の何れの消化槽でも揮発性有機酸の残留は認められておらず、嫌気性処理反応は問題なく進行していたものと考えられる。 In any of the digestive tanks of the comparative example and the example, no volatile organic acid remained, and it is considered that the anaerobic treatment reaction proceeded without any problem.
上記の比較例１および２、実施例１および２で得られた嫌気性消化汚泥を用いて、汚泥脱水処理性能を検討した。汚泥脱水にはカチオン性高分子凝集剤（平均分子量３００万）を用いた。また、脱水機はベルトプレス式脱水機を用い、脱水処理条件は、ろ布緊張力４．９ｋＮ／ｍ、ろ布スピード１．０ｍ／分で行った。 Using the anaerobic digested sludge obtained in Comparative Examples 1 and 2 and Examples 1 and 2, the sludge dewatering performance was examined. A cationic polymer flocculant (average molecular weight of 3 million) was used for sludge dewatering. Further, a belt press type dehydrator was used as the dehydrator, and the dehydration conditions were a filter cloth tension of 4.9 kN / m and a filter cloth speed of 1.0 m / min.
先ず、比較例１および２の嫌気性消化汚泥について脱水処理した結果、高分子凝集剤注入率と脱水ケーキ含水率は表４の結果であった。 First, as a result of dehydrating the anaerobic digested sludges of Comparative Examples 1 and 2, the polymer flocculant injection rate and the dehydrated cake moisture content were the results shown in Table 4.
次に、実施例１および２で得られた嫌気性消化汚泥について脱水処理した結果、高分子凝集剤注入率と脱水ケーキ含水率の結果は表５の結果であった。何れの脱水方法でも従来法よりも高性能であったが、中でも、図４に示される凝集剤を２回に分けて注入して生物処理水を併用する処理方式では最も効率的であることが分かる。なお、実施例１で得られた嫌気性消化汚泥を分離水で希釈することなく、そのままの状態で高分子凝集剤を注入して汚泥を凝集・脱水処理した場合は、高分子凝集剤注入率３．８％（対ＳＳ）、脱水ケーキ含水率８３％であった。 Next, as a result of dehydrating the anaerobic digested sludge obtained in Examples 1 and 2, the results of the polymer flocculant injection rate and the dehydrated cake moisture content were the results shown in Table 5. Either dehydration method has higher performance than the conventional method, but among them, the treatment method in which the flocculant shown in FIG. 4 is injected in two portions and combined with biologically treated water is most efficient. I understand. When the anaerobic digested sludge obtained in Example 1 was not diluted with separated water, the polymer flocculant was injected as it was and the sludge was coagulated and dehydrated. It was 3.8% (vs. SS) and the water content of the dehydrated cake was 83%.
［実施例３］
次に、図５に基づいて、下水汚泥と食品製造廃棄物（廃糖液およびデザート系廃製品）と河川敷刈草の嫌気性処理を行った実施例について示す。[Example 3]
Next, based on FIG. 5, it shows about the Example which performed the anaerobic process of the sewage sludge, food manufacturing waste (waste sugar liquid and dessert-type waste product), and riverbed cut grass.
＜処理条件＞
・下水汚泥量（初沈汚泥と余剰汚泥の混合汚泥） ３０ｍ３／日（ＴＳ濃度３．１％）
・食品製造廃棄物搬入量 １．３５ｔ／日（ＴＳ濃度９．９％）
・河川敷刈草搬入量 ０．１５ｔ／日（含水率７０．０％）
・バイオマス貯槽 ３ｍ３×２槽
＜前処理固液分離装置（下水混合汚泥用）＞
・スリット型濃縮機（スクリーンスリット幅１．０ｍｍ、背圧板付帯）
・カチオン性高分子凝集剤（平均分子量３００万）注入率０．４％（対ＳＳ比）
・汚泥濃縮物量 １２ｔ／日（ＴＳ濃度７．９％）
・分離液量 １９．５ｍ３／日（ＳＳ濃度３９５ｍｇ／Ｌ）
・ＳＳ回収率９７％
・刈草用粉砕装置
＜嫌気性消化：可溶化および酸発酵装置（縦型機械式攪拌機）＞
・食品製造廃棄物、河川敷刈草、汚泥濃縮物の混合物の可溶化および酸発酵装置への投入量３ｍ３／日（スラリーＴＳ濃度１０％）
・汚泥濃縮物のＴＳに対する食品製造廃棄物・河川敷刈草のＴＳ比 １９％
・ＨＲＴ ２日
・有効容積６ｍ３
・水温４５℃
＜嫌気性消化：嫌気性消化装置（縦型機械式攪拌機）＞
・嫌気性消化装置への投入量１３．５ｍ３／日
・ＨＲＴ １４．８日
・有効容積２００ｍ３
・水温３７℃
＜嫌気性消化汚泥の凝集処理工程＞
・スリット型濃縮機（スクリーンスリット幅１．０ｍｍ）
・汚泥分離液の混合量 １０．５ｍ３／日（Ｍアルカリ度６９０ｍｇＣａＣＯ３／Ｌ）
・生物脱臭装置廃液の混合量 ３．５ｍ３／日（Ｍアルカリ度１２５０ｍｇ／Ｌ）
・カチオン性高分子凝集剤（平均分子量３００万）注入率１．７％（対ＳＳ比）
（注入率内訳；前段凝集槽の注入率１．３％、再凝集槽の注入率０．４％）
＜脱水機＞
・スクリュープレス型脱水機
＜発電機＞
・マイクロガスタービン発電機
＜処理結果＞
・嫌気性消化汚泥性状（ＴＳ濃度３．９％、ＶＴＳ６８％、ＳＳ濃度３．０％、Ｍアルカリ度８９００ｍｇＣａＣＯ３／Ｌ、粗浮遊物含有率１６．７％（対ＳＳ比））
・バイオガス発生量 ５７０ｍ３／日（ＮＴＰ）
・メタンガス発生量 ３６５ｍ３／日（ＮＴＰ）
・メタンガス濃度 ６４％
・メタンガス発生率 ０．３７ｍ３／投入ｋｇＶＴＳ（ＮＴＰ）
・バイオガス中のシロキサンＤ５濃度 ２．３ｍｇ／ｍ３
・発電量 ６８６ｋｗｈ／日
・脱水ケーキ発生量 ２．１ｔ／日（含水率７７％）
・廃水量 ３７．６ｍ３／日<Processing conditions>
・ Sewage sludge volume (mixed sludge of initial settling sludge and excess sludge) 30 m 3 / day (TS concentration 3.1%)
・ Food manufacturing waste carried in 1.35t / day (TS concentration 9.9%)
-Riverbed cut grass carry-in amount 0.15t / day (water content 70.0%)
・ Biomass storage tank 3m 3 × 2 tank <Pretreatment solid-liquid separator (for sewage mixed sludge)>
・ Slit type concentrator (screen slit width 1.0mm, with back pressure plate)
-Cationic polymer flocculant (average
・ Amount of sludge concentrate 12t / day (TS concentration 7.9%)
-Separation liquid volume 19.5m 3 / day (SS concentration 395mg / L)
・ SS recovery rate 97%
・ Crusher for grass cutting <Anaerobic digestion: Solubilization and acid fermentation equipment (vertical mechanical stirrer)>
・ Solubilization of a mixture of food manufacturing waste, riverbed grass, sludge concentrate, and input to acid fermentation equipment 3m 3 / day (
-TS compared to TS of sludge concentrate, TS of food processing waste and
・
・ Water temperature 45 ℃
<Anaerobic digestion: Anaerobic digester (vertical mechanical stirrer)>
・ Input amount to anaerobic digester 13.5m 3 / day ・ HRT 14.8 days ・ Effective volume 200m 3
・ Water temperature 37 ℃
<Aggregating treatment process of anaerobic digested sludge>
・ Slit type concentrator (screen slit width 1.0mm)
・ Mixed amount of sludge separation liquid 10.5m 3 / day (M alkalinity 690mgCaCO 3 / L)
・ Mixing amount of biological deodorization equipment waste liquid 3.5m 3 / day (M alkalinity 1250mg / L)
-Cationic polymer flocculant (average
(Breakdown of injection rate: 1.3% injection rate for the previous agglomeration tank, 0.4% injection rate for the re-agglomeration tank)
<Dehydrator>
・ Screw press type dehydrator <Generator>
・ Micro gas turbine generator <Process results>
・ Aerobic digested sludge properties (TS concentration 3.9%, VTS 68%, SS concentration 3.0%, M alkalinity 8900mgCaCO 3 / L, crude suspended solid content 16.7% (vs. SS ratio))
・ Biogas generation amount 570m 3 / day (NTP)
・ Methane gas generation amount 365m 3 / day (NTP)
・ Methane gas concentration 64%
・ Methane gas generation rate 0.37m 3 / kg kg VTS (NTP)
-Siloxane D5 concentration in biogas 2.3 mg / m 3
・ Power generation amount 686kwh / day ・ Dehydrated cake generation amount 2.1t / day (water content 77%)
・ Amount of wastewater 37.6m 3 / day
以上のように、本発明によって従来よりも大幅に小型化した嫌気性消化装置によって汚泥や有機性廃棄物を嫌気性処理して良質なバイオガスを安定的に発生せしめることができ、バイオガス発電できることも明らかとなった。従来法のＨＲＴ２０〜３０日での処理方式では嫌気性消化槽６３０〜９４５ｍ３を設ける必要があったのに対して、本発明では２０６ｍ３の嫌気性消化装置であるので嫌気槽規模は従来の１／３〜１／４に縮小されたシステムで嫌気性処理が可能である。さらには、発生した嫌気性消化汚泥は容易な操作によって低コストで凝集・脱水でき、得られた脱水ケーキ含水率７７％は従来の８２％程度と比較して低含水率であり（表４参照）、外観も従来品と変わりなく、不快臭もなく衛生的であった。As described above, anaerobic digesters that are significantly smaller than conventional ones according to the present invention can anaerobically treat sludge and organic waste to stably generate high-quality biogas. It became clear that we could do it. Whereas in the processing method of the conventional method of
［実施例４］
実施例３と同様に、図５に基づいて、下水処理場において下水汚泥と食品製造廃棄物（ジュース用の蜜柑絞り粕）の嫌気性処理を行った。下水汚泥は重力濃縮した初沈濃縮汚泥と余剰汚泥の混合汚泥として、汚泥濃縮を実施した。嫌気性消化は下水汚泥と蜜柑絞り粕の各固形物量をほぼ等量の混合比率で実施した。[Example 4]
Similarly to Example 3, based on FIG. 5, anaerobic treatment of sewage sludge and food production waste (tangerine juice for juice) was performed in a sewage treatment plant. As sewage sludge, sludge concentration was performed as a mixed sludge composed of gravity-concentrated primary sedimentation sludge and excess sludge. Anaerobic digestion was carried out at a mixing ratio of approximately equal amounts of solids of sewage sludge and mandarin orange pomace.
＜処理条件＞
・下水汚泥量（初沈汚泥と余剰汚泥の混合汚泥） ３５ｍ３／日
（初沈汚泥： ＴＳ濃度３．８８％、余剰汚泥： ＴＳ濃度０．９３％、混合汚泥： TS濃度１．３９％）
・食品製造廃棄物搬入量 ４．０ｔ／日（ＴＳ濃度１２．５％）
・バイオマス貯槽 ３ｍ３×２槽
＜前処理固液分離装置（下水混合汚泥用）＞
・スリット型濃縮機（スクリーンスリット幅１．０ｍｍ、背圧板付帯）
・カチオン性高分子凝集剤（平均分子量３００万、溶液濃度２．０ｇ／L）注入量０．９５ｍ３／日
・高分子凝集剤注入率 ０．４４％（対ＳＳ比）
・汚泥濃縮物量 ６．２ｔ／日（ＴＳ濃度７．５％）
・分離液量 ２９．８ｍ３／日（ＳＳ濃度２３０ｍｇ／Ｌ）
・ＳＳ回収率９８％
＜食品製造廃棄物の可溶化・酸発酵装置＞
・６．０ｍ３×１槽、縦型機械攪拌機、３７℃加温
・汚泥濃縮物のＴＳに対する食品製造廃棄物のＴＳ比 １０２％
＜嫌気性消化装置（縦型機械式攪拌機）＞
・嫌気性消化装置への投入量１０．２ｍ３／日
・ＨＲＴ １９．６日
・有効容積２００ｍ３
・水温３７℃
＜嫌気性消化汚泥の凝集処理工程＞
・スリット型濃縮機（スクリーンスリット幅１．０ｍｍ）
・汚泥分離液の混合量 ２．０ｍ３／日（Ｍアルカリ度３２０ｍｇＣａＣＯ３／Ｌ）
・カチオン性高分子凝集剤（平均分子量３００万）注入率１．６％（対ＳＳ比）
・凝集剤注入工程 1回
＜脱水機＞
・スクリュープレス型脱水機
＜発電機＞
・マイクロガスタービン発電機
＜処理結果＞
・嫌気性消化汚泥性状（ＴＳ濃度３．８％、ＶＴＳ７０％、ＳＳ濃度３．２％、Ｍアルカリ度４４９０ｍｇＣａＣＯ３／Ｌ、粗浮遊物含有率 １２．１％（対ＳＳ比））
・バイオガス発生量 ５９１ｍ３／日（ＮＴＰ）
・メタンガス発生量 ３４９ｍ３／日（ＮＴＰ）
・メタンガス濃度 ５９％
・メタンガス発生率 ０．３８ｍ３／投入ｋｇＶＴＳ（ＮＴＰ）
・バイオガス中のシロキサンＤ５濃度 １．２ｍｇ／ｍ３
・発電量 ６５６ｋｗｈ／日
・脱水ケーキ発生量 １．６ｔ／日（含水率７８％）
・廃水量 ４１．５ｍ３／日<Processing conditions>
・ Sewage sludge volume (mixed sludge of primary sludge and surplus sludge) 35 m 3 / day (primary sludge: TS concentration 3.88%, surplus sludge: TS concentration 0.93%, mixed sludge: TS concentration 1.39% )
・ Amount of food manufacturing waste carried in 4.0t / day (TS concentration 12.5%)
・ Biomass storage tank 3m 3 × 2 tank <Pretreatment solid-liquid separator (for sewage mixed sludge)>
・ Slit type concentrator (screen slit width 1.0mm, with back pressure plate)
-Cationic polymer flocculant (average
-Sludge concentrate amount 6.2t / day (TS concentration 7.5%)
-Separation liquid amount 29.8m 3 / day (SS concentration 230mg / L)
・ SS recovery rate 98%
<Solubilization / acid fermentation equipment for food manufacturing waste>
・ 6.0m 3 × 1 tank, vertical mechanical stirrer, 37 ℃ heating ・ TS ratio of food manufacturing waste to TS of sludge concentrate 102%
<Anaerobic digester (vertical mechanical stirrer)>
・ Input amount to anaerobic digester 10.2 m 3 / day ・ HRT 19.6 days ・ Effective volume 200 m 3
・ Water temperature 37 ℃
<Aggregating treatment process of anaerobic digested sludge>
・ Slit type concentrator (screen slit width 1.0mm)
・ Mixed amount of sludge separation liquid 2.0m 3 / day (M alkalinity 320mgCaCO 3 / L)
-Cationic polymer flocculant (average
・ Coagulant injection process once <Dehydrator>
・ Screw press type dehydrator <Generator>
・ Micro gas turbine generator <Process results>
・ Aerobic digested sludge properties (TS concentration 3.8%, VTS 70%, SS concentration 3.2%, M alkalinity 4490 mgCaCO 3 / L, crude suspended solid content 12.1% (vs. SS ratio))
・ Biogas generation amount 591m 3 / day (NTP)
・ Methane gas generation amount 349m 3 / day (NTP)
・ Methane gas concentration 59%
・ Methane gas generation rate 0.38m 3 / input kg VTS (NTP)
・ Siloxane D5 concentration in biogas 1.2mg / m 3
・ Power generation amount 656 kwh / day ・ Dehydrated cake generation amount 1.6 t / day (water content 78%)
・ Amount of wastewater 41.5m 3 / day
以上のように、本発明による下水汚泥濃縮では、機械濃縮してない重力濃縮のみの初沈濃縮汚泥および余剰汚泥の混合生汚泥に対して（TS濃度１．３９％）、TS濃度７．５％にまで効率的に濃縮処理でき（汚泥濃縮倍率約５．４倍）、従来から多く適用されている各種機械濃縮設備を省略することが可能である。そして、本発明では大幅に小型化した嫌気性消化装置で濃縮汚泥と蜜柑絞り粕の各固形物量をほぼ等量の混合比率で嫌気性消化処理しても良質なバイオガスを安定的に発生せしめることができる。さらには、発生した嫌気性消化汚泥は実施例３と同様に容易な操作によって低コストで凝集・脱水でき、得られた脱水ケーキ含水率７８％は従来と比較して低含水率である。 As described above, in the sewage sludge concentration according to the present invention, the TS concentration is 7.5 with respect to the mixed raw sludge of the primary sedimentation sludge and the excess sludge that are not mechanically concentrated but only gravity concentrated (TS concentration 1.39%). % (Sludge concentration ratio is about 5.4 times), and it is possible to omit various mechanical concentration facilities that have been widely applied conventionally. And in the present invention, a highly miniaturized anaerobic digester can stably generate high-quality biogas even if anaerobic digestion treatment is performed with an approximately equal mixing ratio of each solid content of concentrated sludge and mandarin be able to. Furthermore, the generated anaerobic digested sludge can be agglomerated and dehydrated at low cost by the same easy operation as in Example 3, and the resulting dehydrated cake moisture content of 78% is lower than that of the prior art.
［実施例５］
実施例３及び４で発生した廃液および脱水ケーキについて、有効利用を検討した。本発明の前処理工程にあたる下水汚泥の固液分離から発生した分離液および脱水工程の脱水分離液からはリンの回収、嫌気性消化汚泥濃縮物の脱水工程から発生した脱水ケーキについてはコンポスト化した。[Example 5]
The waste liquid and dehydrated cake generated in Examples 3 and 4 were examined for effective use. Recovery of phosphorus from the separated liquid separated from the solid-liquid separation of the sewage sludge and the dehydrated cake generated from the dehydrated process of the anaerobic digested sludge concentrate were composted. .
＜処理条件＞
（１）汚泥の固液分離廃液のリン回収（MAP法）
・反応時のｐＨ８．３、Ｍｇ濃度を３０ｍｇ／ｌ以上
・１槽式リアクタ（反応部：直径３５ｃｍ×高さ２．２ｍ、沈殿部：直径８０ｃｍ×高さ１．８ｍ、粒径約０．４〜１．０ｍｍの種晶を予め充填）
・リン容積負荷２０ｋｇ−Ｐ／ｍ３・日
（２）脱水ケーキのコンポスト化
・コンポスト化試験装置 １５ｍ３（高速堆肥化縦型発酵槽）
・脱水汚泥の水分調整 汚泥を機械乾燥して含水率４５〜５５％
・副資材添加ナシ
・コンポスト化時の通気速度０．１５ｍ３／ｔ・分
＜処理結果＞<Processing conditions>
(1) Phosphorus recovery from sludge solid-liquid separation waste liquid (MAP method)
-PH 8.3 at the time of reaction, Mg concentration is 30 mg / l or more-1 tank type reactor (reaction part: diameter 35 cm x height 2.2 m, precipitation part: diameter 80 cm x height 1.8 m, particle size of about 0.1 mm) Pre-filled with 4 to 1.0 mm seed crystals)
・ Phosphorus load 20kg-P / m 3・ Day (2) Composting dehydrated cake ・ Composting test equipment 15m 3 (High-speed composting vertical fermenter)
・ Moisture control of dewatered sludge Moisture content of 45-55% by mechanical drying of sludge
・ No auxiliary material added ・ Air ventilation speed at composting 0.15m 3 / t ・ min <Process result>
以上のように、本発明において実施例３及び４で発生した廃液からはリン回収され、脱水ケーキについてはコンポスト化できて品質上も従来製品（比較例として生ごみ系中温メタン発酵汚泥のコンポスト性状を列挙）と殆ど変わりないことも明らかとなった。コンポスト化にける有機物分解率は、実施例３の汚泥で２４％、実施例４では２８％だった。なお、脱水ケーキの高位発熱量は、実施例３の汚泥で１７ＭＪ／ｋｇ−ｄｒｙ、実施例４の汚泥では１７．３ＭＪ／ｋｇ−ｄｒｙであることから、この脱水汚泥を機械乾燥して汚泥燃料としても有効活用できる品質である〔燃料化物（造粒乾燥化物）の品質基準として、発熱量４０００ｋａｌ／ｋｇ以上（１６．７ＭＪ／ｋｇ以上）とされている〕。 As described above, phosphorus is recovered from the waste liquid generated in Examples 3 and 4 in the present invention, and the dehydrated cake can be composted, and in terms of quality, it is a conventional product (compost properties of garbage-type intermediate temperature methane fermentation sludge as a comparative example) It is also clear that there is almost no change. The organic matter decomposition rate in composting was 24% for the sludge of Example 3 and 28% for Example 4. The high calorific value of the dewatered cake is 17 MJ / kg-dry for the sludge of Example 3, and 17.3 MJ / kg-dry for the sludge of Example 4. Therefore, the dewatered sludge is mechanically dried to obtain sludge fuel. As a quality standard for fueled products ( granulated and dried products), the calorific value is 4000 kal / kg or more (16.7 MJ / kg or more).
１…汚泥、２…貯留槽、３…凝集槽、４…凝集剤、５…凝集汚泥、６…前処理汚泥濃縮槽、７…汚泥濃縮物、７ａ・・・消化汚泥、８…分離液、９…嫌気性消化槽、９ａ…可溶化および酸発酵処理槽、１０…バイオガス、１１…嫌気性消化汚泥、１２…消化汚泥凝集装置、１２ａ…汚泥凝集処理槽、１２ｂ…再濃縮凝集汚泥調製装置、１２ｃ…凝集汚泥、１２ｄ…濃縮凝集汚泥、１４Ａ…凝集汚泥分離濃縮装置、１５…消化汚泥凝集物、１３、１３ａ、１３ｂ…凝集剤、１４…分離液、１５…消化汚泥凝集物、１６…脱水装置、１７…分離液、１８…脱水ケーキ、１９…生物処理水、２０…有機性廃液または廃棄物、２１…バイオマス貯槽、１０１…バイオガスタンク、１０２…ガス利用設備、１０３…余剰ガス燃焼設備、１０４…廃水処理設備。
DESCRIPTION OF SYMBOLS 1 ... Sludge, 2 ... Storage tank, 3 ... Coagulation tank, 4 ... Coagulant, 5 ... Coagulated sludge, 6 ... Pretreatment sludge concentration tank, 7 ... Sludge concentrate, 7a ... Digested sludge, 8 ... Separation liquid, DESCRIPTION OF
Claims (7)
該凝集槽からの該凝集汚泥を汚泥濃度４〜１２wt％の汚泥濃縮物と分離液とに固液分離する前処理汚泥濃縮装置、
該前処理汚泥濃縮装置からの該汚泥濃縮物を嫌気性消化するとともにバイオガスを回収する嫌気性消化装置、
該嫌気性消化装置で調製された、Ｍアルカリ度が４４９０〜８９００ｍｇ／ｌおよびＳＳに対する粗浮遊物含有率が５〜１８％である嫌気性消化汚泥に、凝集剤と、前記分離液とを混合して希釈し、Ｍアルカリ度が２５００〜４０００ｍｇ／ｌの消化汚泥凝集物を調製する消化汚泥凝集装置、
該消化汚泥凝集物を固液分離して得られる消化汚泥濃縮物を脱水する脱水装置、および
該前処理汚泥濃縮装置からの該分離液を該消化汚泥凝集装置へ送る配管
を含む、嫌気性処理方法を行う嫌気性処理装置。 A coagulation tank for preparing coagulated sludge by adding a coagulant to the sludge,
A pretreatment sludge concentrator for solid-liquid separation of the agglomerated sludge from the agglomeration tank into a sludge concentrate having a sludge concentration of 4 to 12 wt% and a separation liquid;
Anaerobic digester that anaerobically digests the sludge concentrate from the pretreatment sludge concentrator and collects biogas;
The flocculant and the separation liquid are mixed with anaerobic digested sludge prepared with the anaerobic digester and having an M alkalinity of 4490-8900 mg / l and a crude suspended solid content of 5-18% for SS. A digested sludge agglomeration device for preparing a digested sludge agglomerate having a M alkalinity of 2500 to 4000 mg / l,
An anaerobic treatment comprising a dehydrator for dewatering a digested sludge concentrate obtained by solid-liquid separation of the digested sludge aggregate, and a pipe for sending the separated liquid from the pretreatment sludge concentrate to the digested sludge agglomerator Anaerobic treatment device performing the method.
外部から搬入した有機性廃液または廃棄物を貯留する外部バイオマス貯留装置と、該外部バイオマス貯留装置から排出されるバイオマスを、前記汚泥貯留装置、可溶化および酸発酵処理する装置、及びメタン発酵処理する装置からなる群から選択される少なくとも１つに導入する機構及び配管を備える請求項５又は６の嫌気性処理装置。 The anaerobic digestion apparatus includes a device for solubilizing and acid fermentation treatment of the sludge concentrate, and a device for methane fermentation treatment of digested sludge treated with the device,
External biomass storage device for storing organic waste liquid or waste carried from the outside, and biomass discharged from the external biomass storage device, the sludge storage device, the device for solubilization and acid fermentation treatment, and the methane fermentation treatment The anaerobic treatment apparatus according to claim 5 or 6, further comprising a mechanism and a pipe for introduction into at least one selected from the group consisting of apparatuses.
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| JP6432226B2 (en) * | 2014-09-05 | 2018-12-05 | 栗田工業株式会社 | Method and apparatus for anaerobic digestion of sewage treatment sludge |
| JP6715187B2 (en) * | 2014-12-25 | 2020-07-01 | 水ｉｎｇ株式会社 | Method and apparatus for treating oil-containing wastewater |
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| JP6666346B2 (en) * | 2015-07-21 | 2020-03-13 | 水ｉｎｇ株式会社 | Organic substance processing method and processing apparatus |
| CN109071267A (en) * | 2016-04-11 | 2018-12-21 | 凯米拉公司 | Improve the sludge dewatering ability and energy balance of wastewater treatment |
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